Carbon-based durable goods and renewable fuel from biomass waste dissociation for transportation and storage

ABSTRACT

Techniques, systems, apparatus and material are described for generating renewable energy from biomass waste while sequestering carbon. In one aspect, a method performed by a reactor to dissociate raw biomass waste into a renewable source energy or a carbon byproduct or both includes receiving the raw biomass waste that includes carbon, hydrogen and oxygen to be dissociated under an anaerobic reaction. Waste heat is recovered from an external heat source to heat the received raw biomass waste. The heated raw biomass waste is dissociated to produce the renewable fuel, carbon byproduct or both. The dissociating includes compacting the heated raw biomass waste, generating heat from an internal heat source, and applying the generated heat to the compacted biomass waste under pressure.

CROSS-REFERENCE TO RELATED APPLICATION(S)

The present application is a continuation of U.S. application Ser. No.13/584,733 filed Aug. 13, 2012, now U.S. Pat. No. 8,916,735, whichapplication claims priority to and the benefit of U.S. ProvisionalPatent Application No. 61/523,280, filed Aug. 13, 2011, and entitled“CARBON-BASED DURABLE GOODS AND RENEWABLE FUEL FROM BIOMASS WASTEDISSOCIATION FOR TRANSPORTATION AND STORAGE,” the entirety of bothapplications are incorporated by reference herein.

BACKGROUND

This application relates to devices, techniques and materials related tocarbon sequestration and renewable energy production from biomass waste.

Aquatic plants and vegetative groundcover, particularly farms andforests, are essential carbon dioxide collectors, natural habitats forcountless wildlife, and sources of fiber for applications ranging frompaper products to building materials. Devastation of forests on almostall continents has occurred because of non-native pest introductions andgreenhouse gas exacerbated climatic changes that have made forestsvulnerable to pestilence, fire, wind, flood, and drought damages.

Throughout South, Central, and North America forest fires have destroyedvast stands of trees that have been weakened or killed by drought anddisease. This represents an enormous loss of pulp and buildingmaterials. Fires and rot also produce greenhouse gases such as carbondioxide and methane that further harm the global atmosphere. It is ofparamount importance to provide practical solutions that enable rapidconversion of vegetative biomass into renewable supplies of fuels,electricity, and valuable materials before these materials are lostbecause of fires, decay, floods and erosion. A corollary objective is tofacilitate rapid redevelopment of healthy forests, crops, and othergroundcover and to facilitate production of fuel and sequestered carbonvalues from prescribed thinning and underbrush removal to improve forestconditions and to prevent the spread of harmful fires.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 shows a process flow diagram of a process for a rapid conversionof carbon and hydrogen containing biomass wastes into useful renewablesources of carbon and hydrogen that can be used to produce carbon-baseddurable goods and renewable fuel.

FIG. 2 shows an exemplary system for dissociating biomass waste intohydrogen and carbon carrying intermediaries.

FIG. 3 shows a system for rapid conversion of biomass wastes intorenewable fuel and carbon products.

FIG. 4 is a process flow diagram of a process for dissociatinghydrocarbons and alcohols to obtain carbon and hydrogen.

FIG. 5 shows an exemplary process for producing DME from methanol.

FIG. 6 is a block diagram of a system for generating carbon-baseddurable goods from biomass waste produced hydrocarbons and alcohols.

FIG. 7 shows a system for separating mixtures of product gases such ascarbon dioxide and carbon monoxide from methane and/or hydrogen bypressure swing or temperature absorption.

FIG. 8 is a system for separating methanol from carbon monoxide andshipment of the separated methanol to market by delivery pump.

FIG. 9 illustrates another system for providing biomass waste materialconveyance and compaction.

FIG. 10 is a process flow diagram showing a process for convertingmethane from landfills, sewage treatment plants, waste disposaloperations and other methane sources into hydrogen and carbon.

FIG. 11 is a diagram showing another efficient system for facilitatinghydrogen production with carbon repurposing or recycling.

FIG. 12 is a block diagram showing an overall process for usingphotosynthesis to convert biomass to renewable fuel and sequestercarbon.

FIG. 13 is a block diagram showing another process for usingphotosynthesis to initiate production of valuable fuels, solvents,chemical precursors, and a wide variety of sequestered carbon productsfrom biomass.

FIGS. 14A and 14B are diagrams showing a solar concentrator for usingsolar energy to provide heat to the biomass conversion process.

FIG. 15 is a process flow diagram showing a process for transportingrenewable energy generated from biomass wastes, including municipal,farm, and forest wastes such as forest slash and diseased and/or deadtrees.

FIG. 16A is a process flow diagram showing a process for producingcarbon-based and other durable goods and renewable fuels from organicfeedstocks, which can be stored and transported.

FIG. 16B is an alternative process flow diagram showing a wet-processfor producing carbon-based and other durable goods and renewable fuelsfrom organic feedstocks

FIG. 17A is a process flow diagram showing a process for producingcarbon-based and other durable goods and renewable fuels from organicfeedstocks, which can be stored and transported.

FIG. 17B is an alternative process flow diagram showing a process forproducing carbon-based and other durable goods and renewable fuels fromorganic feedstocks, which includes an in-line filter.

FIG. 18 is a process flow diagram showing global warming resolution inaccordance with an example of the disclosure.

FIG. 19 is a process flow diagram showing global warming resolution inaccordance with an example of the disclosure.

Like reference symbols and designations in the various drawings indicatelike elements.

DETAILED DESCRIPTION

Techniques, materials, apparatus and systems are described forrepurposing carbon and hydrogen present in biomass waste to producedurable goods and renewable fuel. The described techniques, materials,apparatus and systems can reduce or eliminate release of harmful carboninto the environment. For example, the described techniques, apparatus,systems and materials can be used to produce carbon-based durable goods,renewable fuels, electricity, valuable chemicals, soil nutrients, andmaterials from organic feedstocks particularly including energy cropsand wastes. The described techniques can also be used for redevelopmentof forests and other vegetative groundcover that have been destroyed bydisease, fire, and other harmful events.

Overview

Techniques, structures, apparatus and materials are disclosed forgenerating renewable energy, such as biofuels from biomass whilesequestering carbon. Described are methods and systems for anaerobic(e.g., thermochemical) production of efficiently pressurized, refinedand conveniently delivered feedstocks and products such as hydrogen,methane and carbon along with soil nutrients from biomass wastesincluding enormous amounts of agricultural and forest wastes.

In one aspect, a method performed by a reactor to dissociate raw biomasswaste into a renewable source of energy or a carbon byproduct or bothincludes receiving the raw biomass waste that includes carbon, hydrogenand oxygen to be dissociated under an anaerobic reaction. Waste heat isrecovered from an external heat source to heat the received raw biomasswaste. The heated raw biomass waste is dissociated to produce therenewable fuel, carbon byproduct or both. The dissociating includescompacting the heated raw biomass waste, generating heat from aninternal heat source, and applying the generated heat to the compactedbiomass waste under pressure.

Implementations can optionally include one or more of the followingfeatures. Recovering the waste heat can include at least one ofrecovering heat rejected from an engine or fuel cell, and generatingheat from a renewable energy generator including at least one of a windenergy generator, a solar energy generator, an energy generator fromrunning water and a geothermal energy generator. The method can includeadvancing the compacted biomass waste towards a dissociation zone fordissociating the compacted biomass waste and removing moisture and airfrom the advancing compacted biomass waste. Removing the moisture andair can include extruding the compacted biomass waste through a confinedspace to physically squeeze the moisture and air out. The method caninclude forcing the produced renewable fuel or carbon byproduct or bothin a counter-flow direction from the advancing compacted biomass wasteand transferring heat from the produced renewable energy, carbonbyproduct or both that travel in the counter-flow direction. Therenewable fuel can include at least one of hydrocarbon, alcohol,ammonia, and hydrogen. The carbon byproduct can include at least one ofcarbon dioxide, carbon monoxide and carbon. The method can includeproducing a durable good using the carbon produced from the biomasswaste. The hydrocarbon can include at least one of methane, propane,ethane and butane. The alcohol can include at least one of methanol,propanol, ethanol and butanol. The method can include separating thehydrocarbon into hydrogen and carbon. Also, the method can includeproducing a durable good using the carbon produced from the biomasswaste. The raw biomass waste can include organic material containingcarbon and hydrogen obtained in response to photosynthesis. The methodcan include applying a catalyst to facilitate formation of the renewableenergy comprising a hydrocarbon. The catalyst can include at least oneof, chromium, ceramics with rare earth constituents, a platinum metalgroup, nobleized nickel, and intermetallics of transition metals. Thebiomass waste can include at least one of fructose, lipid, carbohydrate,protein, glucose, lignin, and cellulosic feedstock.

In another aspect, the described methods can be implemented using asystem for production of a fuel mixture from biomass waste materialincludes a hopper to receive raw biomass waste material to be convertedto the fuel mixture comprising a hydrocarbon. A countercurrent heatexchanger is coupled to the hopper to recover waste heat from a heatsource and provide the recovered heat to the hopper to heat the rawbiomass waste material. A pressurized and heated reactor is coupled tothe hopper to receive the heated raw biomass waste material and performvarious operations. For example, the reactor includes a conveyor toapply an extrusion action to the heated raw biomass waste material toobtain a compacted biomass waste material. Also, the reactor includes acombustor to transfer heat to the compacted biomass waste material toproduce the hydrocarbon containing fuel mixture using a thermochemicalreaction.

Implementations can optionally include one or more of the followingfeatures. The external heat source can include a device for generatingrenewable energy comprising at least one of a wind energy generator, asolar energy generator, an energy generator from running water and ageothermal energy generator. The conveyor can be configured to advancethe compacted biomass waste towards a dissociation zone for dissociatingthe compacted biomass waste; and remove moisture and air from theadvancing compacted biomass waste. The conveyor can include aprogressively reduced pitch of helical flights of rotating tubes on anexterior surface of the conveyor to facilitate the removal of moistureand air. The pressurized and heated reactor can be shaped to reduce across sectional area within the reactor for advancing the compactedbiomass waste material while facilitating the removal of moisture andair. The system can include a countercurrent heat exchanger coupled tothe reactor to transfer heat from the produced renewable fuel, carbonbyproduct or both to the compacted biomass waste that travels in acounter-flow direction from the advancing compacted biomass waste. Therenewable fuel can include at least one of hydrocarbon, alcohol, ammoniaand hydrogen. The carbon byproduct can include at least one of carbondioxide, carbon monoxide and carbon. The hydrocarbon can include atleast one of methane and ethane. The alcohol can include at least one ofmethanol and ethanol. The system can include a hydrocarbon conversionsystem that includes one or more heat exchangers coupled to the reactorto receive the hydrocarbon and further coupled to the heat source toreceive heat used to separate the hydrocarbon into hydrogen and carbon.The raw biomass waste can include organic material containing carbon,hydrogen and oxygen obtained in response to photosynthesis. The systemcan include a catalytic reaction zone for receiving a catalyst tofacilitate formation of the renewable fuel comprising a hydrocarbon. Thecatalyst can include at least one of chromium, ceramics with rare earthconstituents, a platinum metal group, nobleized nickel, andintermetallics of transition metals. The biomass waste can include atleast one of glucose, lignin, and cellulosic feedstock.

The subject matter described in this specification potentially canprovide one or more of the following advantages. For example, thedescribed techniques, systems and materials can convert biomass intoenergy while recycling and repurposing environmentally harmfulgreenhouse gases, such as carbon dioxide. Also, the describedtechniques, systems and material can be used to convert biomass intoenergy with high energy-conversion efficiency and moderate costs forcapital equipment and infrastructure improvements. The describedtechniques also can be scaled up to tackle large biomass sources, suchas forest conversion while reducing operating costs. Moreover, thedescribed techniques can minimize or eliminate releases of carbondioxide.

Biomass Waste Dissociation

FIG. 1 shows a process flow diagram of a process 100 for a rapidconversion of carbon and hydrogen containing biomass wastes into usefulrenewable sources of carbon and hydrogen that can be used to producecarbon-based durable goods and renewable fuel.

A system (e.g., a biomass dissociation system 200 below) can subdividethe biomass waste into feedstock materials such as various cellulosicmaterials and lignocellulosic tissues (110). The subdivided feedstockmaterials can be compacted to remove air and moisture (120). Thecompacted biomass waste feedstock can be heated to release varioususeful renewable sources of carbon and/or hydrogen including carbon,hydrogen, hydrocarbons, alcohols, ammonium, and oxides of carbon (130).Also, the moisture content of the overall reaction environment can becontrolled based on the desired amounts and/or proportions of renewablecarbon and/or hydrogen (140). To control the moisture content, thecompacted biomass waste feedstock that has been dried and de-aired canbe used as a desiccant, for example. The renewable sources of hydrogenand carbon can be used to generate renewable fuel and/or carbon-baseddurable goods (150).

For example, as shown in Equation 1, biomass wastes can be heatedsufficiently in an anaerobic environment to release desirable gases,carbon, and solid residues such as mineral oxides and other compounds.The anaerobic process for oxides of carbon and co-production of hydrogenand/or hydrocarbons from biomass wastes summarized in Equation 1 is notbalanced for any particular type, amount, or ratio of lignin, cellulose,or other biomass feedstock.C_(x)H_(y)O_(z)+HEAT→C+H₂+CH₄+H₂+CO₂+CO  (1)

Using the process described in Equation 1, virtually any organicmaterial can be converted in large part to hydrocarbon fuel, such asmethane (CH₄) for distribution and storage in the existing natural gasinfrastructure. Equation 2 below illustrates a general summary of theoverall reactions for production of a hydrocarbon such as methane fromtypical biomass wastes such as glucose, lignin, and cellulosicfeedstocks.C₆H₁₂O₆+HEAT→3CH₄+3CO₂  (2)

In some implementations, the biomass dissociation reaction can producealcohols, such as methanol, ethanol or butanol as a readily storable andtransportable liquid fuel and chemical precursor. Methanol or “woodalcohol” can be extracted by heating lignocellulosic wastes throughpartial combustion or by anaerobic heating processes. Equations 3 and 4summarize the output of methanol that can be achieved by selection ofdifferent anaerobic operating temperatures, pressures, and catalysts.C₆H₁₂O₆+HEAT→6CO+6H₂  (3)6CO+6H₂→3CH₃OH+3CO  (4)

At higher feed rates and/or lower heat release rates in a reactor, thecharge does not reach the higher temperatures that produce the gasesshown in Equation 1, and thus the dissociation process produces alcohol,such as methanol. Carbon monoxide can be separated from methanol bycooling the methanol vapors to form liquid methanol and to utilize theseparated carbon monoxide to fuel a combustion engine, to release heatthrough combustion by a burner assembly, and to form hydrogen by areaction with water as summarized in Equation 5. Hydrogen produced bythe reaction summarized in Equation 5 may be used to produce methanol asshown in Equation 4, to improve operation of an engine, to improve theyield of methane and/or ethane in the biomass conversion and/or as aheating fuel.CO+H₂O→H₂+CO₂  (5)

FIG. 2 shows an exemplary system 200 for dissociating biomass waste 202into hydrogen and carbon carrying intermediaries. The system 200includes a biomass waste 202 intake component, such as a hopper 210 thatreceives the biomass waste 202 in raw form and breaks down (e.g., chips,chops, grinds, etc.) the raw material into subdivided feedstock, such asvarious cellulosic and lignocellulosic materials. The hopper 210 caninclude a heating mechanism, such as a heat exchanger 212 to pre-heatthe subdivided feedstock. The heat exchanger can recapture and recyclewaste heat from an external heat source (e.g., engine exhaust and/orrenewable heat, such as wind, solar, running water, geothermal, etc.) orfrom the reactor 220.

The subdivided (and in some implementations, pre-heated) feedstock 214is forwarded to a reactor 220 to dissociate the biomass waste feedstock214 into useful renewable sources of carbon and hydrogen, such asvarious hydrocarbons, alcohols, ammonia, and oxides of carbon. Thereactor can include a drying mechanism 222 to expel moisture and airfrom the feedstock. The drying mechanism 222 can include an extrudingdevice to physically ‘squeeze out’ the moisture and air from thefeedstock. Examples of the extruding device include a helical screwconveyor and a ram piston conveyor. Also, the drying mechanism 222 caninclude one or more heating mechanisms, such as heat exchangers thatcapture heat generated by the reactor 220 and recycle the captured heatto dry the feedstock. The heat exchangers can also recapture and recyclewaste heat from an external heat source (e.g., engine exhaust and/orrenewable heat, such as wind, solar, running water, geothermal, etc.)

The reactor 220 can also include a heating mechanism 224 for generatingadequate heat used in an anaerobic reaction to dissociate the biomasswaste feedstock 214 into the useful renewable sources of carbon andhydrogen 216, such as hydrocarbons, alcohols, ammonia and oxides ofcarbon. The generated useful renewable sources of carbon and hydrogen216 can be forwarded to a storage and/or transport mechanism 230 to beused in additional reactions to generate renewable fuel and/orcarbon-based durable goods in respective reactions as described inprocesses (400 and 500) and systems (600 and 700) described below.Moreover, the storage and/or transport mechanism 230 allows forefficient transport of the useful renewable sources of carbon andhydrogen 216 to remote locations for further processing.

The reactor 220 can be configured to increase thermal efficiency of thebiomass waste 202 conversion process while reducing or eliminatingcarbon dioxide formation. For example, the reactor 220 can includemechanisms to perform various countercurrent drying (e.g., recyclingheat) and elimination of air, moisture, and other oxygen donors prior toextraction of carbon, hydrocarbons such as methane, and/or hydrogen.

FIG. 3 shows a biomass waste dissociation system 300 that uses a helicalscrew mechanism to expel moisture and air from the biomass wastefeedstock. In operations, waste heat from an engine cooling systemand/or exhaust gases can be transferred to the raw biomass materials ina hopper 350 by countercurrent turns of helical heat exchange tubing 344and 345 that are joined to the hopper 350 at respective zones thatderive the maximum amount of heat recovery from the engine 302. Theheated raw biomass materials are advanced to a pressurized and heatedreactor 311 for dissociation into a mixture that includes hydrocarbons,hydrogen and carbon products. The heated reactor 311 includes a biomasscompactor 314, such as a rotating tubular screw conveyor within astationary containment tube 336 that compacts the raw biomass waste to adense state and advance the compacted biomass waste towards adissociation or reaction zone near a combustor assembly 320. Therotating tubular screw conveyor can include helical flight tubes 318 onan exterior surface of the rotating tubular screw conveyor 314 toprovide an extrusion action on the compacted biomass waste.

The rotating tubular screw conveyor 314 can be driven by suitable speedreduction systems 304 and 306 through an engine 302. Based on the sizeof the system 300 and throughput desired, the engine 302 can mayimplemented as a rotary, reciprocating piston, or turbine engine withsuitable exhaust/intake systems 328. The system 300 can obtainimprovements in overall efficiency for generation of electricity by asuitable generator such as alternator 380 connected to the engine 302.Also, the engine 302 can be fueled by a fuel conditioning, injection,and ignition system as disclosed in U.S. Pat. No. 6,155,212, the entirecontents of which is incorporated herein by reference.

Depending on the size of the converter system 300 implemented to convertthe biomass wastes to renewable energy, speed reduction components suchas sprockets and a chain or a drive gear 306 and bearing supportassembly 308 and 312 can be thermally isolated from the rotating tubularscrew conveyor 314 and housing 342 by a torque-conveying thermalinsulator assembly including 312, 310, and 326. The rotating tubularscrew conveyor 314 is supported similarly and thermally isolated at anopposite end by insulated bearing and support assembly 324 and 326 asshown. An insulator pack 330 provides insulation to prevent radiativeand conductive heat gain by bearing 312 and other areas where protectionfrom heat is desired.

To continuously compact the raw solid biomass materials that areentrained within the stationary tube 336, the system 300 can include adrying mechanism to remove moisture and/or air from the biomassmaterial. The drying mechanism can include progressively reduced pitchof the helical flight tubes 318 on the exterior of the rotating tubularscrew conveyor 314 and/or a reduced cross-sectional area between therotating tubular screw conveyor 314 and the stationary tube 336. Thedrying mechanism can provide for expulsion of entrapped air and/ormoisture from the biomass material being heated by the process byforcing the entrapped air and moisture to travel in a counterflowdirection to the material being ingested through the heated hopper 350and a feed screw 356 driven by a suitable traction motor 352 or asuitable drive train from the engine 302. Decreasing the pitch of therotating tubular screw conveyor 314 or reducing the cross sectionthrough which compacted biomass wastes travel can further provide acompact seal to reduce or prevent leakage of gases produced by furtherheating of the organic materials including reactions with additions ofreactive gases.

After successive expulsion of air and moisture, the compacted biomassmaterial is dissociated into carbon and hydrogen and/or the producthydrocarbon gases as shown in Equation 1 at the dissociation or reactionzone using the heat transferred from the combustion device 320. The hotproducts, such as water vapor, nitrogen, oxygen, and carbon dioxide ofthe combustion device 320 are circulated past a spiral heat exchangetubing 316 within tube 314 to transfer heat to the compacted biomassmaterials that travel in a counterflow direction by extrusion action ofthe helical flight tubes 318 located on an exterior surface of therotating tubular screw conveyor 314 as shown.

The dissociation reactions also generate a much lower volume of solidresidues. The amount of solid residue can be about 2 to 10% of theoriginal mass of organic waste. Such residues are important sources oftrace minerals that can be used to revitalize soils and assure rapidgrowth of replacement stands of healthy forests, gardens, aquaculture,and/or other groundcover. This can expedite greenhouse gas reduction,sequestration of carbon and hydrogen, and economic development. Also,reforested areas can serve as sustainable sources of lignocelluloses forcontinued production of renewable methane, hydrogen and sequesteredcarbon.

A relatively small portion of the hydrocarbon (e.g., methane) and/orhydrogen and/or carbon monoxide generated as summarized by Equation 1 isdelivered to the engine 302 and to a burner nozzle of a combustorassembly 320 through a control valve 322 as shown in FIG. 3. Sufficientamount of air is provided to assure complete combustion of fuel valuesthat are present with minimal objectionable emissions in allapplications.

The system 300 can be implemented as larger units and high through-putversions in which combustion gases from the combustor or burner assembly320 may be circulated within tubular flights (e.g., a spiral heatexchange tubing) 316 constructed to connect through holes in therotating tubular screw conveyor 314 with the helical flight tubes 318 toprovide more rapid transfer of heat from combustor 320 to feedstockmaterials progressing along the outside of the helical flight tubes 318within the containment tube 336. Gases such as methane, hydrogen andcarbon dioxide that are released from heated biomass feedstocks by thethermal dissociation process are allowed to pass into an annular spacebetween helical fins or helical flight tubes 338 and insulated tube 341to flow in countercurrent direction to the flow of feedstock beingheated by the rotating tubular screw conveyor 314. This provides forfurther heat conservation as heat is regeneratively added to feedstockswithin the containment tube 336 that are progressively compacted anddissociated by heat transfer to enhance pressure production as shown.

Combustion gases such as water vapor, nitrogen, oxygen, and carbondioxide reaching the hopper area 350 by travel through the interior ofthe rotating tubular screw conveyor 314 and/or tubular fins or tubularflights 316 and/or helical flight tubes 318 enter a helical heattransfer tubing 346 to provide further countercurrent energy addition tothe feedstock materials progressing through the hopper 350 as shown.Gases that are produced such as methane, hydrogen and carbon dioxideand/or carbon monoxide reaching the area of the hopper 350 by passagethrough holes 330 (not shown) and the annular space between thecontainment tube 336 and insulated tube 341 and/or hollow fin 338 arecirculated through a tubing 348 which is wound adjacent to a helicalheat transfer tubing 346 for efficient countercurrent heat transfer tomaterials progressing to the rotating tubular screw conveyor 314 asshown. Insulation 342 and 360 prevent heat loss to the outside.

Such mixtures of product gases are provided at a suitable margin abovethe desired pressure by controlling the speed of rotation of therotating tubular screw conveyor 314 and thus the compaction of solidsthat are delivered to the thermal dissociation stage. This providesefficient conversion of heat energy into pressure energy as desiredgases are formed in substantially larger volumes than the original solidvolume. In operation, a pressure sensor 370 sends pressure data to aprocess controller 372 for maintaining the speed of a feed conveyor 356,the rotating tubular screw conveyor 314, and the heat rate of combustorassembly 320 to achieve desired throughput, conversion temperature, andpressure of delivered product gases. A pressure regulator 374 canprovide the final adjustment of product gas delivery from a regenerativeconverter through a pipeline 376.

The gas mixture produced by operation of the system 300 at approximately1,000 PSI and 1025° F. (69 Atmospheres, 550° C.) can vary as shown inTable 1 with the type of biomass wastes being converted, the dwell time,and related parameters of operation. A new formulation provides forcompression ignition to replace diesel fuel and includes adsorbedhydrogen in activated carbon suspensions in methanol.

TABLE 1 Gas Product Forest Waste Municipal Solid Waste Manure Hydrogen(H₂) 22 (vol %) 33 (vol %) 20 (vol %) Methane (CH₄) 60 53 61 Ethane(C₂H₆) 17 11 18 Carbon Monoxide  1  2  1 (CO)

Such gas mixtures can be rapidly produced and can be supplemented withhigher energy constituents such as methanol, carbon suspensions inmethanol, or propane, butane, ammonia, etc., to achieve virtually anydesired energy content of the resulting hydrogen-combustioncharacterized combustion mixture in combined fuel applications. Also,the hydrogen and/or methane produced by the reaction can be redirectedinto the reaction zone by injection through the manifold 339 at a ratesufficient to produce the desired ratios of methane and ethane toprovide pipeline quality gas or feedstocks for chemical synthesis.

With most biomass wastes, the initial output without recycling hydrogencan range from 350 to 650 BTU/scf in a lower heating value. An increasedheating value can be achieved by various selections of pressure andtemperature in the decomposition process or by increasing the rate thathydrogen is recycled to the reaction zone at the manifold 339.

The carbon to hydrogen ratios of the chemical species produced can becontrolled by implementing a relatively extended period of operationwith greatly reduced carbon production in between times that carbon isintentionally produced to aid in sealing the zone before collection ofdesired chemical species and/or the zone after such collection. Thisenables carbon to be transported as a constituent of fluids that aredelivered by pipeline to storage including repressurization of depletednatural gas reservoirs, to industrial plants for making carbon-enhanceddurable goods, and for other purposes. A system and a method of pipelinedelivery of the produced hydrocarbons, hydrogen and/or carbon productsare described with respect to FIG. 15 below.

The reactions of Equations 1-5 and systems 200 and 300 above may befurther improved by the use of homogeneous and heterogeneous catalystsand application of adaptive controls to improve or optimize the desiredresults. For example, in the reaction zone between the manifold 339 andthe gas stripper ports 340, catalysts can be added to enhancehydrocarbon (e.g., methane and ethane) and alcohol (e.g., methanol andethanol) formation by reactions that facilitate the action of hydrogento build reactive components that synthesize to form such compounds.Examples of catalysts include chromia and other ceramics with rare earthconstituents, the platinum metal group, nobelized nickel, andintermetallics of transition metals. Use of catalysts can provide anunexpected and significant reduction of equipment cost and complexitycompared to conventional approaches. Similarly, lanthanide-rutheniumpreparations, Fischer-Tropsch catalysts, and copper, copperintermetallics, and/or copper alloys can be used to enhance methanolsynthesis from carbon monoxide and hydrogen along with production ofmethanol by partial oxidation of methane.

In another aspect, low cost heat can be converted into potential energyas stored energy and the utilization of such pressure to facilitateseparation processes, and energy regeneration. Pressurized mixtures areseparated while retaining desirable pressurization of selected gases.Such pressurized supplies of refined quality gas can be used to powerengines including internal combustion engines and engines with externalheat supplies.

Such energy conversion, refinement and pressurization are also utilizedto deliver refined gases to distant markets by pipeline or pressurizedtank cars or by condensation, liquefaction, and storage. Also, thedescribed energy conversion, refinement and pressurization can beimplemented to operate in certain areas in conjunction with one or moreof the various embodiments of the U.S. Pat. No. 6,984,305, the teachingsof which are incorporated herein by reference.

The described systems (e.g., systems 100, 300) can provideself-reinforcing structures of tubular construction. Strengthening canbe provided by helical reinforcement structures that combine heatexchange, strengthening, rigidizing, conveying, and heat resistingbenefits in modular structures that can be built by rapid assemblyprocesses. This greatly expedites deployment of the remedies needed inwaste management and reduces the delivered system cost compared toconventional approaches.

Carbon-Based Durable Goods from Dissociation of Hydrocarbons andAlcohols

The hydrocarbons (e.g., methane) and alcohols (e.g., methanol) producedfrom biomass waste as shown with respect to process 100 and systems 200,300 above, can be dissociated to produce carbon for a multitude of“specialized carbon” applications ranging from diamond plating andsemiconductors to composite structures that are stronger than steel andlighter than aluminum. FIG. 4 is a process flow diagram of a process 400for dissociating hydrocarbons and alcohols to obtain carbon andhydrogen. A reactor (e.g., reactor 610) can receive hydrocarbons andalcohols dissociated from biomass waste (410). The reactor can applyadequate heat and pressure to the hydrocarbons and alcohols todissociate carbon from hydrogen (420). Equation 6 illustrates a generalprocess of dissociating hydrocarbon fuel to obtain hydrogen and/ormethane and carbon. Equation 7 shows a specific reaction fordissociation of methane into carbon and hydrogen.C_(x)H_(y)+HEAT₄→XC+0.5YH₂  (6)CH4+▴H_(298K)→2H₂+C(▴H_(298K)=79.4 kJ/mol)  (7)

Equation 8 shows a reaction for dissociating cellulose and fuel alcoholsthat contain oxygen by anaerobic decomposition to obtain carbon, carbonmonoxide and hydrogen.C₂H₅OH+HEAT→C+CO+3H₂  (8)

The carbon monoxide can be reacted in an anaerobic reaction shown inreversible Equation 9 to increase the yield of hydrogen from feedstocksthat contain carbon, hydrogen and oxygen:CO+H₂O→CO₂+H₂+HEAT  (9)

Total energy value of hydrogen and carbon monoxide produced in theendothermic reactions (e.g., Equation 1) can be 15 to 20% greater thanthat of methane used to source the carbon monoxide and hydrogen.

To increase the thermochemical efficiency of the reactions, the heatused to dissociate the hydrocarbons can be harvested and recycled fromengine exhaust (e.g., waste heat) or a renewable energy source, such assolar energy or heat released by combustion of a suitable fuel includingproducts generated by reactions of Equations 1-5.

The carbon dissociated in the processes can be collected for use in theproduction of carbon-based durable goods (430). For example, the carbonextracted from biomass waste-produced hydrocarbons and alcohols can beused to generate carbon products including activated carbon, fibrouscarbon, diamond-like coatings, graphitic components, and carbon black.These forms of carbon products can be used to manufacture durable goods,such as better equipment to harness solar, wind, moving water, andgeothermal resources along with transportation components that arestronger than steel and lighter than aluminum. Recycling or repurposingcarbon to produce equipment that harnesses renewable resources providesmany times more energy than burning such carbon one time. Makingcarbon-enhanced durable goods and equipment can provide highlyprofitable business benefits compared to the greenhouse gases andpollution produced by burning carbon.

Also, the hydrogen co-produced with carbon from the dissociation ofhydrocarbons and alcohols can be collected for use in producing variousrenewable fuels (440).

In some implementations, the anaerobic reaction can be modified toproduce intermediate chemicals, such as dimethyl ether (DME) and/ordiethyl ether (DEE) from dissociation of the biomass waste producedincluding intermediates (ethylene, propylene etc.) and/or alcohols(e.g., methanol, ethanol, butanol, etc). FIG. 5 shows an exemplaryprocess 500 for producing DME from methanol or DEE from ethanol. Areactor (e.g., reactor 610) can receive alcohols dissociated frombiomass waste (510). The reactor can apply adequate heat and pressure tothe alcohols to generate DME and/or DEE and water (520). Equation 10shows an illustrative specific reaction for DME production frommethanol.2CH₃OH→CH₃OCH₃+H₂O  (10)

The generated DME can be converted by de-hydration into polymerprecursors, such as ethylene or propylene, which are building blocks forplastics, such as polyethylene, polypropylene and other polymers (530).Equation 11 shows a process for de-hydration of DME to obtain ethyleneor propylene.CH₃OCH₃→C₂H₄+H₂O  (11)

The above generated ethylene or propylene can be used to generatepolymers (540). The polymers can be used to produce carbon-based durablegoods (550). Converting methanol into polymers such as polyethyleneand/or polypropylene by the processes described effectively sequestersthe CO₂, resulting in a net removal of CO₂ from the atmosphere.

FIG. 6 is a block diagram of a system 600 for generating carbon-baseddurable goods from biomass waste produced hydrocarbons and alcohols. Thesystem 600 includes a reactor 610 that receives the biomass wasteproduced hydrocarbons and alcohols 216 from the storage and transportmechanism 230 (from FIG. 2.) The reactor 610 can include a heatingmechanism 612, such as heat exchangers for applying the heat used in theanaerobic reactions of Equations 6-8. The carbon 616 dissociated fromthe hydrocarbons and alcohols are used in production of durable goods630.

The reactor 610 can also include a drying mechanism 614 for de-hydratingthe alcohols to create DEE or DME 618, which can be used to produceethylene or propylene 635. Also, the heating mechanism 612 can be usedto dehydrate the alcohols and/or their products DEE and/or DME. Theproduced ethylene or propylene can be used to generate polymers forproducing various plastics and other carbon-based durable goods 630.

In addition, the anaerobic reaction generated in the reactor 610produces hydrogen 619 in addition to the carbon 616 from the hydrocarbonand alcohol dissociation. The dissociated hydrogen 619 can be stored atthe storage & transport mechanism 640, such as a container and/or apipeline. Also, the hydrogen produced can be used to generate renewablefuel using a renewable fuel generating system (e.g., 700).

Separation of CO₂ and CO from Hydrocarbons and Hydrogen

Referring back to Equation 1, the biomass waste dissociation can producehydrogen, oxides of carbon and hydrocarbons, such as methane.C_(x)H_(y)O_(z)+HEAT→CH₄+H₂+CO₂+CO  (1)

The oxides of carbon can be separated from the hydrocarbons and hydrogenfor use in separate reactions. FIG. 7 shows an exemplary system 700 forseparating mixtures of product gases such as carbon dioxide and carbonmonoxide from methane and/or hydrogen by pressure swing or temperatureabsorption. This provides for efficient separation of carbon compoundssuch as carbon dioxide or carbon monoxide from gases such as methaneand/or hydrogen. For example, mixtures of product gases are deliveredthrough a tube 704 and travels along helical fins 706 as shown in FIG. 7to be exposed to water or other absorber fluid selections in a pressurevessel 702 for selective separation of carbon dioxide and/or carbonmonoxide.

Methane and/or hydrogen are thus delivered to a collection tube 708 asthe pressure is maintained in a pressure vessel 702. After absorption ofcarbon dioxide and/or carbon monoxide, the pressurized absorption fluidis delivered by a pipe 710 to a nozzle manifold 726 for delivery to heatexchangers such as 714, 716, 718, 720, 722, 724, etc. Heat from theexhaust of the engine 302 in FIG. 3 may be delivered to the heatexchangers 714, 716, 718, 720, 722, 724, etc. Additional heat can bedelivered to the heat exchangers 714, 716, 718, 720, 722, 724, etc.,including the heat released by a burner 744 from combustion of portionsof the produced gas along with waste gases such as carbon monoxide thatis released through outlet 758 by subsequent expansion of thepressurized fluid. Additional heat may also be supplied by a solarcollector 742 or by resistance or induction heaters using wind, movingwater, or geothermal energy where such resources are abundant. Heatedfluids are then expanded across turbines 730, 732, 734, 736, 738, 740,etc., as shown for recovery and/or conversion of energy to furtherimprove overall efficiency.

In addition, the heated fluids can be recycled through a vessel 750 toremove heat from the heated liquid using a heat exchanger/coolingcircuit 756 that circulates water or other materials through inlet andoutlet ports 746 and 748 to take heat away from the heated fluid. Insome implementations, the methane and/or hydrogen separated from theoxides of carbon can react with an oxygen donor circulated through theheat exchanger/cooling circuit 756 to generate water. The generatedwater and/or cooled fluid can pass through a port 752 and forwarded tothe pressurized vessel 702 using a pump 754.

The system 700 in FIG. 7 can provide additional improvements in overallefficiency in generation of electricity by a suitable generator such asan alternator 728. Hydrogen can be used to cool these generators andreduce windage losses. After performing these functions, the samehydrogen can be then used to fuel the engine 302 or as a carbon-freefuel in combustor (e.g., burner) 744 and/or 320.

In some implementations, carbon dioxide production can be reduced oreliminated by electrolysis of derivatives of the feedstock such as acidsthat are generated to produce oxygen. Hydrogen gasification of suchmaterials particularly with hydrogen and surplus carbon present can alsobe controlled to produce ethane in simultaneous or subsequent processes.This chemical process variation can be implemented when it is desired torapidly convert damaged forests into pressurized supplies of methane,ethane, and hydrogen that are shipped to distant markets by pipeline.Then, the pipeline can be used to continue delivery of such gases atreduced rates as a function of desired rates of forest thinning,scheduled harvesting, and maintenance programs.

Pipeline capacity established by this approach becomes an importantstorage system for meeting daily and seasonal variations in marketdemand. It is generally desired for the resultant pipeline gas toprovide about 900 BTU/scf., after removal of carbon dioxide,particulates, ash, sulfur dioxide, and water as shown in FIGS. 1 and 2.

Moreover, thermal dissociation of organic substances to directly producehydrogen and/or to produce methane for distribution and production ofspecialized carbon products as shown above can be far more profitableand can reduce or eliminate costly changes to existing infrastructurethan conventional sequestration and storage of CO₂ after it has beenproduced by wasteful burning of organic materials. The describedtechniques, systems, apparatus and materials can couple carbonsequestration with production with renewable energy.

In addition to co-production by dissociation of hydrocarbon (CxHy)compounds, hydrogen can be derived by electrolytic splitting of waterusing any clean, alternative energy source. Hydrogen can be derived froma non-CO₂ producing anaerobic dissociation of organic materials and/orby utilization of energy sources such as wind, hydro, biomass, solar,tidal, geothermal, or off-peak nuclear power plants. Hydrogen can alsobe produced from virtually any biomass waste that ordinarily rots orburns. Also, carbon-neutral liquid compounds for storage of hydrogen canbe synthesized from hydrogen and carbon dioxide.

Separation of Methanol from Carbon Monoxide

FIG. 8 is a system 800 for separating methanol from carbon monoxide andshipment of the separated methanol to market by delivery pump 830. Inoperation, the system 800 performs vortex separation of denser fromlighter components and provides for mixtures of carbon monoxide andmethanol to enter a separator vessel or chamber 802 by a tube 804 andthrough a port 810 from regenerative pump/motor 812. The regenerativepump/motor 812 provides pumping action on such vapors if the deliverypressure is not adequate to achieve the delivery rate desired andprovides recovery of pressure energy if the desired delivery pressure isless than the supply pressure from the system 100 of FIG. 1 or anothersuitable converter 820.

A heat exchange circuit 806 can be included to provide the cooling usedto condense methanol. The heat exchange circuit 806, which issymbolically shown in FIG. 8, can utilize ground water or cooling towerfluid as a heat sink. The water in the heat exchange circuit 806 can bemaintained at a higher pressure by a pump 840 than the vapors that enterthe separator chamber 802, and thus any containment failure of the heatexchange circuit does not cause cooling water contamination. The coolingwater that exits the separator chamber 802 from a port 814 may be usedas a heated water supply or returned to the ground water system, coolingtower, or evaporation pond as appropriate for the application. Aftersufficiently cooling the gas mixture to create denser vapors anddroplets of methanol near the walls of the separator chamber 802, lessdense carbon monoxide is extracted by a central tube 808. Condensedmethanol may be delivered by the delivery pump 830 for furtherprocessing to remove water and/or absorbed gases depending upon thepurity desired.

Methanol and pipeline gas mixtures of methane, ethane, and hydrogen maybe interchangeably shipped to market by the same or additionalpipelines. In instances that the same pipeline is used it is preferredto changeover from one chemical type to the other by proven technologiessuch as the use of a pressure propelled separation slug or by pump downto clear the pipeline before refilling with the next selection to bedelivered.

Biomass Conversion to Hydrocarbon Using Other Mechanisms

Other material conveyance and compaction means can be used to deliverand process biomass wastes. For example, in some implementations, aunidirectional ram delivery and compaction system can be used ratherthan the helical conveyor shown in FIG. 1. Other means can beimplemented for processing the biomass wastes to provide the followingoperations: 1) compaction of the biomass wastes; 2) heat addition toeliminate air and moisture; 3) creating a plug seal of advancingmaterial derived from the feedstock; 4) heating the advancing materialto achieve the desired pressure and temperature conditions fordissociation to produce the desired chemical derivatives selected fromsubstance options such as carbon, one or more vaporous hydrocarbons,fuel alcohols, and gases such as ethane, methane, hydrogen, and oxidesof carbon; and 5) extraction of the desired chemical species in a zonethat utilizes derivatives and/or remnants of the advancing material toseal or help seal the zone that provides for removal of desired chemicalspecies. To maximize heat utilization in the resulting system, the heatadded to the material advancing through such stages of progress can beobtained from countercurrent heat exchanges from the desired chemicalspecies as it is recuperatively or regeneratively cooled. Additionally,the heat added to the material can be obtained by countercurrent heatexchanges from combustion of selected fuels.

FIG. 9 illustrates an embodiment 900 similar to the system 300 of FIG. 3that includes a ram piston compactor 902 for conversion of biomass suchas an energy crop, and/or wastes such as sawdust, manure, and woodchips. This system 900 can operate essentially the same as the 300 ofFIG. 3 except the compaction of biomass is cyclically provided by areciprocating ram. A ram piston compactor 902 can be forced by ahydraulic cylinder 906 to reciprocate in a stationary cylinder 918 tocompact the biomass waste that has been dried and preheated bycountercurrent heat exchange in the hopper 350.

The biomass waste is loaded by the conveyor 356 into stationary cylinder918 when the ram piston compactor 902 is in the position shown. Theengine 302 drives a hydraulic pump 904 (not shown) to deliver apressurized working fluid through lines 910 and 911 to actuate thehydraulic cylinder 906. In the forward stroke, the ram piston compactor902 forces the biomass waste into a dense charge that is furthercompacted as it moves around a cone 912 of a heater 916 which may bestationary or rotated to enhance throughput and maintain the compactionof biomass that is progressing through the conversion process. Numeroustubes in positions typical to manifold 339 allow expulsion of air andwater vapor while further serving as a material check-valve to preventbackward flow of material that is advanced by the action of the rampiston 902. Countercurrent heat exchange from combustion gases fromburner assembly 320 that travel through tubular flights 316 and helicalflight tubes 318 raise the temperature of the biomass sufficiently tocause the dissociation reactions summarized in Equations 1, 2, 3, and 4in response to coordination and control by controller 372.

Thus, the biomass materials can be converted into fluids such asmethane, ethane, propane, methanol, ethanol, hydrogen, hydrogen sulfide,carbon monoxide, and carbon dioxide. Also, the biomass conversion asdescribed above can produce renewable energy that can replace fossilfuels while removing objectionable levels of hydrogen sulfide, carbonmonoxide, and carbon dioxide using the regenerative system 700 of FIG. 7or by another suitable selective removal process such as pressure swingabsorption, temperature swing absorption, solution absorption, andmembrane separation. The renewable fuel production and carbon recyclingor repurposing can be obtained using countercurrent heat exchange fromsources such as combustion of a portion of one or more fuel constituentsfrom such fluids, heat exchange from higher temperature to lowertemperature substances before, during, and after production, and by heatexchange with energy conversion devices such as internal combustionengines, external combustion engines, expansive motors, and fuel cells.

FIG. 10 is another process flow diagram showing a process 1000 forconverting methane from landfills, sewage treatment plants, wastedisposal operations using the systems 100, 200, 300, 700, 800 and 900 asdescribed with respect to FIGS. 1, 2, 3, 7, 8 and 9 along with othermethane sources into hydrogen and carbon as summarized in Equations 6-7above. Hydrogen combusts seven to nine times faster compared tohydrocarbons such as gasoline, fuel alcohols, methane, and diesel fuel.This enables improved thermal efficiency in biomass conversion coupledwith reduction or elimination of carbon emissions by turbine, rotarycombustion, and reciprocating engine operations in which hydrogen orhydrogen-characterized fuels such as mixtures of hydrogen and methane,hydrogen and methanol, or hydrogen and carbon monoxide are injected andignited.

Improvements in thermal efficiency gained by above described operationsare particularly important for intermittent combustion engines such asrotary combustion engines and reciprocating two- or four-stroke enginessuch as 302 whereby direct injection and/or ignition is provided closeto, at, or after top dead center to reduce or prevent heat loss andbackwork during compression. This assures much greater efficiency in theconversion of fuel potential energy to work energy during the powerstroke of the engine. Thus, by combusting fast burninghydrogen-characterized fuel within surplus air in the combustionchamber, considerably greater operating efficiencies can be achievedcompared to engines with conventional arrangements to utilize propane,natural gas or diesel fuels.

The hydrocarbons, such as methane, produced and purified to the desireddegree using the systems 100, 200, 300, 700, 800 and 900 of FIGS. 1, 2,3, 7, 8 and 9 are transported by bulk carrier or pipeline to a suitabledestination such as an industrial park (process 1010). The transportedhydrocarbons are then preheated from ambient temperature to a suitabletemperature such as about 1200° C. (2200° F.) by countercurrent heatexchange from hydrogen and/or carbon that is produced by dissociation(process 1020). Sufficient heat is added by radiation and/or contactwith a heated substance such as graphite, iron oxide, aluminum oxide,magnesium oxide, various carbides or other ceramics to cause carbon tobe precipitated on or near such heated substance selections and hydrogenis released as summarized by Equations 2, 6 or 7 (process 1030). Theheated hydrogen is collected for countercurrent heat exchange withadvancing methane as described with respect to process 1020 (process1040). Carbon that is formed by dissociation of methane is collected asa deposit or as a powder or flake material that is stripped orexfoliated from the heated substrate used in process 1030 (process1050).

In some implementations, a portion of the carbon and/or the hydrogenco-produced in the process 1030 is provided to be combusted to heat orassist with heat addition to produce the desired pressure andtemperature for dissociation of methane (1060). Alternative sources ofheat addition for accomplishing dissociation of methane in process 1030include: 1) concentrated solar energy, 2) electric induction heating ofa conductive ceramic such as graphite or zirconium oxide, 3) resistanceheating of such substrates and radiative heating of such substrates froma suitable incandescent source, 4) various varieties of plasma heatingincluding plasma involving hydrogen and/or methane, 5) and/or bycombustion of a suitable fuel including the methane or the products ofmethane dissociation such as hydrogen and or carbon.

In some implementations, the process 1000 described above can beimplemented using various types of fluidized beds, helical screw orpiston induced flow reactors, plasma chambers with carbon collectionprovisions and features, and improved carbon-black production furnaces.

FIG. 11 is a diagram showing another efficient system 1100 forfacilitating the method of hydrogen production with carbonsequestration. Similar to the above described systems and methods, thesystem 1100 shown in FIG. 11 can be implemented to produce hydrogen fromhydrocarbons, such as methane, with much lower energy addition thanrequired to dissociate water. Moreover, valuable forms of carbon areco-produced with hydrogen.

In operation, a hydrocarbon such as methane is delivered by a pipe 1102to a refractory tubular barrel 1104. Within the refractory tubularbarrel 1104, a refractory conveyor screw 1110 is rotated to moveparticles and/or substrate materials 1111 of preferred geometry and sizeto receive carbon that is dissociated from a hydrocarbon such as methaneand deposited or precipitated as the methane is heated by radiation,conduction etc., according to the process summarized in Equations 6-7.Hydrogen that is co-produced is ducted through holes 1108 of a hollowhelical screw conveyor 1110 to the interior bore as shown. Thus, heatedhydrogen and carbon that travels towards a seal 1114 and exchanges heatwith methane that travels from seal 1126 toward a seal 1114. The helicalscrew conveyor 1110 serves as an energy exchange system for conductiveand radiative heat along with performing mechanical work to rapidlyaccomplish the reactions summarized by Equations 6-7.

A suitable heat source 1106 is used to add heat to the system todissociate the preheated methane. Heat may also be added by combustionof hydrogen within the hollow center of the refractory screw assembly1110 as shown. Oxygen or another oxidant such as air can be deliveredthrough a rotary union 1118 to be used for such combustion. Potentialsource for the oxygen used in hydrogen combustion can include airseparation or electrolysis. Hydrogen can be delivered by a conduit 1117through a rotary union 1119 as shown.

Based on the size of the converter system 1100, speed reductioncomponents such as sprockets and a chain or a drive gear 1132 and abearing support assembly 1130 can be thermally isolated from therotating screw assembly 1110 by a torque-conveying thermal insulatorassembly 1128. Similarly, insulating support of bearing and rotary unionassembly 1116 with the rotary union 1118 on a shaft 1121 is provided tominimize heat transfer from the helical screw assembly 1110. Aninsulator pack 1124 provides heat-transfer blocking to prevent radiativeand conductive heat losses and other areas where protection from heat isneeded.

A relatively small portion of the methane and/or hydrogen and/or carbonmonoxide generated as summarized by Equations 1 and 6-7 is delivered toan engine generator assembly similar to 302 as shown in FIG. 3 toprovide heat and electricity for support operations. The enginegenerator in FIG. 11 can include an electric drive motor 1136, anelectrolyzer and/or an air separator 1144, a pump or compressor 1146,and a generator 1112 as shown. The electric motor 1136 can include agear or sprocket drive 1134 that drive the corresponding gear orsprocket drive 1132 for driving the ram piston.

The system 1100 can include a progressively reduced pitch of helicalflights to continuously compact the solid biomass materials that areentrained within. In addition to the progressively reduced pitch ofhelical flights, the cross-sectional area between the helical rotatingscrew 1110 and the stationary tube barrel 1104 can be reduced in zonesthat serve as plug seals. This forces travel of methane in heat exchangedirection to carbon traveling counter-current towards extrusion throughthe seal 1114 and hydrogen that travels counter-current toward therotary union 1119 within the helical rotating screw 1110 as shown.

Decreasing the pitch of the screw conveyor or reducing the cross sectionnear or at the seals 1126 and 1114 to compact carbon particles or shapesfurther provides for a compact seal against the escape of hydrogen ormethane. In larger applications, the helical rotating screw 1110 may beprovided with slightly reversed pitch in the zone near the seal 1114 tocause compaction of carbon to produce an effective seal against methaneor hydrogen loss.

An insulation system 1124 facilitates efficient countercurrent heatexchange between hydrocarbons such as methane advancing toward the seal1114 and carbon and/or hydrogen advancing toward the seal 1126. A gearor sprocket drive 1132 is thermally isolated from the drive motor 1136,and bearings 1116 and bearing support assembly 1130 are designed forheat isolation and/or elevated temperature service. The helical screwconveyor 1110 and refractory tubular barrel 1104 can be made ofrefractory metals or ceramic material selections such as graphite,carbides, nitrides, intermetallics, and metallic oxides.

The heat added by the heat source 1106 may be by concentrated solarenergy, catalytic or flame combustion, or by electrical heating such asplasma, resistance or inductive principles preferably using renewableelectricity. Oxygen produced by air separator and/or electrolyzer 1144can be stored in an accumulator 1122 and delivered through a pressureregulator 1120. The delivered oxygen can be used when needed to providefor combustion of hydrogen and heat generation for the dissociationprocess such as during times that solar, wind, moving water and otherrenewable resources are not available or not adequate.

Additionally, as shown in FIG. 11, ports 1108 allow hydrogen or othergases to pass through the helical conveyor wall and enter the interiorbore and travel counter current to the feedstock so the cooled hydrogenexits through 117 and the heated feedstock deposits carbon andco-produces hydrogen.

Photosynthesis: Organic Material for Conversion to Renewable Energy

FIG. 12 is a block diagram showing an overall process 1200 for usingphotosynthesis to convert biomass to renewable fuel and sequestercarbon. A system (e.g., systems 100, 200, 300, 700, 800, 900 and/or1100) can use photosynthesis to provide the organic material typicallycontaining carbon, hydrogen, and oxygen for conversion into renewableenergy (process 1210). The system uses anaerobic digestion or pyrolysisor partial oxidation to produce fuel gases such as methane and oxides ofcarbon (process 1220). The system separates the oxides of carbon such ascarbon dioxide from the produced fuel gases (process 1230). The systemcan provide an appropriate filter, pressure swing adsorption,temperature swing adsorption, or selective absorption 1232 to separatemethane and oxides of carbon.

The system preheats the hydrocarbons (e.g., methane) by countercurrentheat exchanges with hydrogen and carbon prior to final heat addition fordissociation as shown (process 1240). Based on the pressure of thepurified fuel gases and the desired pressure for the foregoing preheatprocess 1240, the system can include a pressurizer 1234 to perform oneor more of the following: 1) electrolysis pressurization, 2) mechanicalpump or compressor operation, or 3) pressurizing release from heatedsubstance and/or adsorptive and/or metal hydride systems. Subsequentprovisions for heat addition are selected to specialize products madefrom carbon derived from preheated methane as shown (process 1250).

FIG. 13 is a block diagram showing another process 1300 for usingphotosynthesis to initiate production of valuable fuels, solvents,chemical precursors, and a wide variety of sequestered carbon productsfrom biomass. Using photosynthesis, a system (e.g., system 100, 200,300, 700, 800, 900 and/or 1100) generates organic feedstocks or biomass,such as manure, garbage and sewage (process 1310). The system convertsthe produced biomass by countercurrent regenerative preheating andanaerobic pyrolysis to carbon rich residue and fluids such as methanol,hydrogen, and carbon monoxide (process 1320). Biomass conversion isdescribed above with respect to systems and methods 100, 200, 300, 700,800, 900 and/or 1100 described with respect to FIGS. 1-3, 6-9 and 11above.

The system delivers the gases such as hydrogen and carbon monoxideproduced by anaerobic pyrolysis using a pump 1322 and separated toproduce the desired degree of purification (process 1330). The systemcan include a second pump 1332 to deliver carbon monoxide to beappropriately proportioned by metering pumps 1342 and 1344. The systemcan convert the delivered carbon monoxide into a wide variety ofproducts (processes 1340, 1350 and 1360).

For example, heat can be produced as carbon monoxide dissociates intocarbon and/or produces carbon dioxide (process 1340). Also, heat can bereleased as carbon monoxide is combined with hydrogen to producemethanol (CH₃OH) (process 1350). Additionally, steam can be reacted withcarbon monoxide in a reaction to produce hydrogen (H₂) and carbondioxide (CO₂) (process 1360). Heat released by these exothermicprocesses can be utilized to produce steam used in process 1360, to drybiomass feedstocks before additional heat is provided in process 1320,for heating anaerobic digester 1120 in FIG. 11 to increase the rate ofmethane and/or hydrogen production, in process 1140, and for many otheruseful purposes.

Solar Concentrator: Heat Source for Biomass Conversion

FIGS. 14A and 14B are diagrams showing a solar concentrator 1400 forusing solar energy to provide heat to the biomass conversion process.The solar concentrator 1400 tracks the sun to continuously focus thereflected solar energy received by a mirror 1412 on a receiver zone 1430of a reactor 1414 to produce a high operating temperature. Sufficientconcentration of solar energy is readily achieved by the parabolic,spherical, or arrayed heliostatic mirror 1412 to produce typicaloperating temperatures of 500° C. to 2500° C. as facilitated by thephysical and chemical properties provided by the material andconfiguration specifications of a containment or receiver tube 1430 fortransmission through 1422 to heat the reactor 1414. Along with thestationary receiver tube 1422, the reactor 1414 includes a rotary screwconveyor and extruder tube 1424 with integral helical screw flights 1426that force reactive ingredients such as organic material into thereaction zone. The organic material in the zone is rapidly heated to thehigh temperature by concentrated solar energy.

A stationary base 1404 houses a drive system and provides transfer ofmaterials to and from the reactor 1414. Fuels and feedstocks such aslandfill methane for the reactor 1414 are delivered by a connectedpipeline 1418. A fluid feedstock, such as sewage can be delivered to thereactor 1414 by a different pipeline 1415. Electricity produced ordelivered is transferred by a cable group 1419. Hydrogen and/or otherfluids produced by the reactor 1414 can be delivered to a pipeline 1416for storage and distribution. A movable stage 1406 rotates around acentral vertical axis to provide sun tracking of the reactor 1414 whichis assembled with the mirror 1412. Coordinated rotation around ahorizontal axis 1409 in support 1410 as shown is provided to track thesun and produce point focused solar energy reflected from the mirrorassembly 1412. Organic solids and semisolids to be heated are loadedinto a hopper 1408 which feeds organic solid materials into a screwconveyor 1424, a portion of which is shown in FIG. 14B.

Other forms of renewable heating are readily adapted such as inductiveor resistive heating using electricity from a generator powered bymoving water, wind, wave action, or by an engine using fuel produced bythe operation described herein. Similarly, a portion of the fuelproduced by the reactor 1414 can be combusted to adequately heat zone1430 for accomplishing the reactions of Equations 1, 4 and 6. This groupof alternate heat inputs to the receiver zone 1430 illustrates means tosupplement or replace solar energy as needed to assure continuedoperation in case of intermittent cloud cover or at night.

Supplemental heating or replacement of solar heat for zone 1430 bypartial combustion of the produced hydrogen and/or carbon monoxide canbe accomplished by delivering oxygen through tube 1437 within a bore1431 of a rotary screw tube 1432 from an electrolyzer 1407. Asynergistic benefit is provided by the operation of a heat engine 1403on the landfill methane and/or hydrogen for driving an electricitygenerator 1405. Surplus electricity generating capacity is used toproduce oxygen and hydrogen in the electrolyzer 1407. Hydrogen producedby such operation can readily be stored in a pipeline 1416 for transportand oxygen can be used to greatly improve the process efficiency of heatgeneration by partial combustion of the fuel produced by the reactor1414 and/or in fuel cell power generation applications.

Elimination of nitrogen greatly reduces the cost of hydrogenpurification by condensing or filtering water from the gas mixturewithin the rotary screw tube 1432 when oxygen is used to produce heat bypartial combustion. Tube 1437 delivers oxygen as shown to combust theamount of fuel needed with minimum heat loss and elimination of heatingrequirements for nitrogen which would be present if air is used as anoxidant.

Stationary receiver tube 1422 thus performs the functions of containingorganic feedstocks in an anaerobic condition and transferring energysuch as solar energy to the biomass conveyed into the concentratedheating zone 1430 to facilitate the reactions summarized as follows:C_(n)H_(m)O_(x)+HEAT₁ →xCO+m/2H₂+(n−x)C  (12)C₆H₁₀O₅+HEAT₂→5CO+5H₂+C  (13)

Small amounts of NH₃, H₂S, N₂, and H₂O may also be found in the gaseousproducts with the CO and H₂ that are forced by the compacted solids intothe center bore 1431 of rotary screw tube 1432 as shown. The generatedH₂S can be reacted with iron to form iron sulfide or collected in carbonproduced by the process as hydrogen is released. Fixed nitrogen can becollected as ammonia and sulfur as iron sulfide to be used as soilnutrients along with mineral ash collected.

Solids such as carbon and ash 1436 are extracted from the zone 1430 bythe rotating motion of the rotary screw tube 1432 along the extruderflights 1434 as shown. High temperature insulation 1440 can be used tocover the end of the receiver/reactor 1414 as shown, and an insulatedarea 1442 can provide heat conservation along the countercurrentexchange of heat made between carbon rich solids being extracted by thescrew conveyor 1432 and biomass moving towards the heated zone 1430 ofthe receiver and reactor assembly. During times that solar energy is notavailable, insulator sleeve 1438 is used to cover the zone 1430 and canbe supported and guided to and from the stored position shown bytelescoping tube guides, which are not shown.

Water and other gases removed at early stages of compaction andcountercurrent pre-heating can be vented through louvers or holes 1444to allow extraction through a collection tubes 1443 and 1446. For manyfeedstocks such as manure and sewage, this water generally containsfixed nitrogen and other soil nutrients and preferably is utilized toreplenish soil tilth and productivity.

When pure carbon and pure hydrogen are preferred, the biomass may bepre-treated to remove ash forming materials such as calcium, magnesium,phosphorus, iron, and other minerals. Ash ingredients of biomass areoften wastefully impounded in landfills or allowed to escape to theoceans as effluent is dumped from sewage and garbage disposaloperations. In the described subject matter, ash is readily collectedand returned to useful applications as a soil nutrient. This may beaccomplished by a combination of mechanical separation and dissolutionof the biomass in a suitable solvent to separate ash components.

Another embodiment provides anaerobic digestion of biomass such ascarbohydrates and cellulose according to the following generalreactions:n(C₆H₁₀O₅)+nH₂O+HEAT₃ →n(C₆H₁₂O₆)  (14)n(C₆H₁₂O₆)→3n(CH₄)+3nCO₂+HEAT₁₀  (15)

Soil nutrients captured in the aqueous liquor remaining after theprocesses shown are efficiently transferred to depleted soils by varioustechniques including addition to irrigation water. Carbon dioxide isreadily removed from the products of the process by cooling to producephase change separation or by adsorption in a suitable solvent such aswater. Carbon dioxide is soluble in water to the extent of about 21.6volumes of gas per volume of water at 25 atmospheres pressure and 12° C.(54° F.).

Increasing the pressure and/or decreasing the temperature increases theamount of carbon dioxide dissolved per volume of water. After separationof carbon dioxide from methane, lowering the pressure or increasing thetemperature releases dissolved carbon dioxide.

The amount of heat required in the process of anaerobic dissociation oforganic feedstocks to produce a given amount of sequestered carbon isconsiderably less than the energy required to collect and dissociatecarbon dioxide from the atmosphere. The apparatus required to practicethe process of carbon sequestration from organic feedstocks is far lessinvolved and much simpler and more rugged than would be required toextract carbon dioxide from the atmosphere and to break it into carbonand oxygen.

In the process of converting hydrocarbons including biomass solids andmethane into carbon and hydrogen, the products of dissociation reactionstend to occupy more volume than the reactants. Apparatus 1420 of thereactor 1414 for carrying out these endothermic reactions can readilyseal the reaction zone 1430 with carbon rich material that is compactedby extruder flights 1426 along the inlet to the reaction zone 1430 andwith carbon rich material along extruder flights 1434 of the outlet ofzone 1430 so that the hydrogen and other gases passing out through thebore 1431 may be pressurized to the desired extent and maintained by arotary union and pressure regulation means on the outlet of the bore1431.

Cool methane can be pressurized to the desired delivery pressure ofhydrogen from the reactor 1420 with a suitable pressurization techniqueincluding pressurization by release from adsorptive substrates, phasechange, mechanical compression, and hybridized systems before methaneentry into reactor 1420. If the gases produced in anaerobic digestionare separated by liquefaction, this is readily accomplished byvaporizing the methane to the pressure desired. Pressurization byvarious pumps and compressors 1234 as shown in FIG. 12 may also be usedfor this purpose.

Types of carbon produced can vary based on market demand and thecorresponding temperature and pressure at which the process of carbonsequestration is accomplished. For example, methane may be processed asneeded to produce fibers, carbon black, diamond-like plating on suitablesubstrate, graphite crystals and in many other forms as described inU.S. Pat. Nos. 6,015,065 and 6,503,584, the teachings of both of whichare incorporated herein in their entirety.

Also, to provide heat conservation for certain applications, the screwconveyor 1432 can be designed as a feed path and a preheater withhydrogen being delivered through the bore 1431 and carbon produced bythe reaction in zone 1430 conveyed by appropriately designed extrudertube 1424 in countercurrent heat exchange with the incoming feedstock.This arrangement can provide countercurrent heating of the incomingfeedstock from the inside and from the outside before reaching thereaction zone 1430 by parallel flows of products passing in the oppositedirection of feedstock.

Carbon formed by the reactor 1414 is carried by the screw conveyor 1432in countercurrent heat exchange with the extruder tube 1424 to preheatthe incoming methane and thus increase the overall efficiency and ratethat solar energy completes the process reactions. Hydrogen produced iscollected in the bore 1431 of the tube conveyor 1432 and heat is removedin countercurrent heat exchange with reactants passing towards thereaction zone 1430.

Renewable hydrogen produced can be used in fuel cells or in heat enginesthat clean the air and provide cleaner exhaust than the ambientatmosphere.

Carbon continuously forms a gas-tight seal between the conveyor flights1426 and the inner wall of the tube 1422 as it is produced by theprocess. This seal can be assured by reducing the helical extruder screwflight lead where the greatest compaction is desired. The greatestcarbon compaction and sealing effect can be provided after the materialundergoing conversion to hydrogen passes the reaction zone 1430 on theoutlet in the screw conveyor past the reaction zone 1430.

Conveyance of reactants in the processes shown in FIGS. 14A and 14B canbe performed by other analogous means in addition to the screw conveyorsas shown. For example, the biomass could be forced to the reaction zone1430 by a reciprocating plunger rather than the screw conveyor 1424 andcarbon can be extracted from the hot end by other extraction methodsincluding a chain drive conveyor rather than the screw conveyor 1432.

When producing a liquid fuel or vapors of a solvent such as one or moreturpenes along with other valuable products, the reaction temperaturemay be adjusted to a reduced temperature or the throughput rate of theingredients increased. Useful compounds such as hydrogen, carbon,methanol, biodiesel and turpentine may be produced and collected in thetube bore 1431 as summarized in the equations or a portion of a typicalbiomass waste feedstock with the average compound formula as shownbelow:C₆H₁₀O₅+HEAT₆→CH₃OH+4CO+3H₂+C  (16)

Incorporation of colloidal carbon that hosts adsorbed hydrogen inmethanol provides higher heating value per volume and the ability toprovide compression ignition in applications for renewable diesel fuel.If a greater yield of liquid fuel and/or solvent is desired, carbonmonoxide and hydrogen produced in the typical process of Equation 16 maybe reacted in the presence of a suitable catalyst to produce additionalmethanol and hydrogen.4CO+3H₂→4CH₃OH+H₂+HEAT₁₂  (17)

The rate of biomass delivered into the reaction zone 1430 and the rateof extraction of solid residues by the helical conveyor 1432 can becontrolled by a computer. For example, the computer can adaptivelycontrol the biomass conversion process in response to instrumentation ofthe pressure, temperature, and other indicators of the kind and qualityof products desired in the gas, vapor and solid residue streams.

Carbon monoxide may be decomposed or converted to desired forms ofsequestered carbon by disproportionation as shown by thenon-stoichiometric process summarized in Equation 18:2CO→C+CO₂+HEAT₁₃  (18)

Disproportionation as summarized in Equation 18 is exothermic and can beprovided under various combinations of temperature and pressureconditions including operations at 10-40 atmospheric pressure at 500° C.to 800° C.

For hydrogen production for fuel cells or heat engines that clean theair, carbon monoxide can be reacted with steam in an exothermic reactionto produce hydrogen as shown in Equation 19:CO+H₂O→CO₂+H₂+HEAT₁₄  (19)

Carbon monoxide produced by the processes summarized above can beconverted into numerous products to meet market demand as selected fromprocesses requiring hydrogen and/or carbon production as illustrated.Heat released by the exothermic processes can be used as a part of theheat addition needed for endothermic reactions shown.

A practical process has been described for sequestration of carbon fromthe atmosphere using photosynthesis, collection of photosynthesizedbiomass, and heating the biomass to yield products selected from thegroup including carbon, hydrogen, methanol, turpenes, and ash. Biomasswastes that are ordinarily allowed to rot into the atmosphere and whichcontribute to carbon dioxide and/or methane buildup can now be utilizedto efficiently produce hydrogen, carbon products and soil nutrients.

Tangible, Useful Applications

Analysis of fire, earthquake and mudslide hazards in most damaged forestsettings show that it is highly advantageous to facilitate the solutionpresently disclosed by establishing underground pipelines to transportmethane produced by rapid harvest and conversion of such damaged forestsand/or groundcover. Pipeline shipment of such renewable methane tomarkets now served by natural gas or other fossil fuels can providedramatic reductions in environmental impact from greenhouse gases andfacilitate evolution from present dependence upon fossil energy torenewable energy security.

Also, job development and investor confidence can be bolstered byestablishment of renewable sources of methane that can be delivered bylow cost transport through pipelines. Further improvement can beprovided by development of the “carbon age” that is facilitated byconversion of methane to carbon products as hydrogen is used for cleanenergy applications.

FIG. 15 is a process flow diagram showing a process 1500 fortransporting renewable energy generated from biomass wastes, includingmunicipal, farm, and forest wastes such as forest slash and diseasedand/or dead trees. A biomass processing system (e.g., systems 200, 300,600, 700, 800, 900 and 1100 described in FIGS. 2-3, 6-9 and 11 above)receives the biomass waste for conversion to renewable energy (process1502). For example, the biomass waste from diseased and/or dead treescan be cut, pulled, or otherwise harvested. The biomass processingsystem chips or otherwise subdivides the harvested biomass wastes intobits and pieces for efficient transport and compaction by a conveyorsuch as a belt, ram, or screw conveyor (process 1504). Usingregenerative dissociation, the biomass processing system dries andconverts the subdivided biomass wastes to produce renewable energy andbyproducts including hydrocarbons, alcohol vapors along with methane,hydrogen, and other gases along with solids such as carbon and mineralsthat are introduced by or along with the cellulose and/orlignocellulosic feedstocks (process 1506). The biomass processing systemseparates vapors and gases such as methane and or hydrogen from carbondioxide (process 1508). The generated methane-rich gases can be shippedto remote locations by pipelines or other transport methods such asthose utilized by the natural gas industry (1510). Hydrogen and carbonproducts can be produced from the methane-rich gases either before orafter transporting the methane-rich gases through pipeline delivery(1512). The produced hydrogen can be used as fuel in variousapplications (1514). For example, hydrogen can be used in engines and/orfuel cells to power motor vehicles, to provide heat, for shaft work andelectricity generation, for chemical process applications, and toproduce fertilizers.

While this specification contains many specifics, these should not beconstrued as limitations on the scope of any invention or of what may beclaimed, but rather as descriptions of features that may be specific toparticular embodiments of particular inventions. Certain features thatare described in this specification in the context of separateembodiments can also be implemented in combination in a singleembodiment. Conversely, various features that are described in thecontext of a single embodiment can also be implemented in multipleembodiments separately or in any suitable subcombination. Moreover,although features may be described above as acting in certaincombinations and even initially claimed as such, one or more featuresfrom a claimed combination can in some cases be excised from thecombination, and the claimed combination may be directed to asubcombination or variation of a subcombination.

Similarly, while operations are depicted in the drawings in a particularorder, this should not be understood as requiring that such operationsbe performed in the particular order shown or in sequential order, orthat all illustrated operations be performed, to achieve desirableresults. In certain circumstances, multitasking and parallel processingmay be advantageous. Moreover, the separation of various systemcomponents in the embodiments described above should not be understoodas requiring such separation in all embodiments.

Only a few implementations and examples are described and otherimplementations, enhancements and variations can be made based on whatis described and illustrated in this application.

To the extent not previously incorporated herein by reference, thepresent application incorporates by reference in their entirety thesubject matter of each of the following materials: U.S. patentapplication Ser. No. 12/857,553, filed on Aug. 16, 2010, now U.S. Pat.No. 8,940,265, and titled “SUSTAINABLE ECONOMIC DEVELOPMENT THROUGHINTEGRATED PRODUCTION OF RENEWABLE ENERGY, MATERIALS RESOURCES, ANDNUTRIENT REGIMES”; U.S. patent application Ser. No. 12/857,541, filed onAug. 16, 2010, now U.S. Pat. No. 9,231,267, and titled “SYSTEMS ANDMETHODS FOR SUSTAINABLE ECONOMIC DEVELOPMENT THROUGH INTEGRATED FULLSPECTRUM PRODUCTION OF RENEWABLE ENERGY;” U.S. patent application Ser.No. 12/857,554, filed on Aug. 16, 2010, now U.S. Pat. No. 8,808,529, andtitled “SYSTEMS AND METHODS FOR SUSTAINABLE ECONOMIC DEVELOPMENT THROUGHINTEGRATED FULL SPECTRUM PRODUCTION OF RENEWABLE MATERIAL RESOURCESUSING SOLAR THERMAL;” U.S. patent application Ser. No. 12/857,502, filedon Aug. 16, 2010, now U.S. Pat. No. 9,097,152, and titled “ENERGY SYSTEMFOR DWELLING SUPPORT,” U.S. patent application Ser. No. 13/027,235,filed on Feb. 14, 2011, now U.S. Pat. No. 8,313,556, and titled“DELIVERY SYSTEMS WITH IN-LINE SELECTIVE EXTRACTION DEVICES ANDASSOCIATED METHODS OF OPERATION;” U.S. Provisional Application No.61/401,699, filed on Aug. 16, 2010 and titled “COMPREHENSIVE COSTMODELING OF AUTOGENOUS SYSTEMS AND PROCESSES FOR THE PRODUCTION OFENERGY, MATERIAL RESOURCES AND NUTRIENT REGIMES;” U.S. patentapplication Ser. No. 13/027,208, filed on Feb. 14, 2011, now U.S. Pat.No. 8,318,131, and titled “CHEMICAL PROCESSES AND REACTORS FOREFFICIENTLY PRODUCING HYDROGEN FUELS AND STRUCTURAL MATERIALS, ANDASSOCIATED SYSTEMS AND METHODS;” U.S. patent application Ser. No.13/026,996, filed on Feb. 14, 2011, now U.S. Pat. No. 9,206,045, andtitled “REACTOR VESSELS WITH TRANSMISSIVE SURFACES FOR PRODUCINGHYDROGEN-BASED FUELS AND STRUCTURAL ELEMENTS, AND ASSOCIATED SYSTEMS ANDMETHODS;” U.S. patent application Ser. No. 13/027,015, filed on Feb. 14,2011 and titled “CHEMICAL REACTORS WITH RE-RADIATING SURFACES ANDASSOCIATED SYSTEMS AND METHODS;” U.S. patent application Ser. No.13/027,244, filed on Feb. 14, 2011 and titled “THERMAL TRANSFER DEVICEAND ASSOCIATED SYSTEMS AND METHODS;” U.S. patent application Ser. No.13/026,990, filed on Feb. 14, 2011, now U.S. Pat. No. 8,187,549, andtitled “CHEMICAL REACTORS WITH ANNULARLY POSITIONED DELIVERY AND REMOVALDEVICES, AND ASSOCIATED SYSTEMS AND METHODS;” U.S. patent applicationSer. No. 13/027,181, filed on Feb. 14, 2011, now U.S. Pat. No.8,187,550, and titled “REACTORS FOR CONDUCTING THERMOCHEMICAL PROCESSESWITH SOLAR HEAT INPUT, AND ASSOCIATED SYSTEMS AND METHODS;” U.S. patentapplication Ser. No. 13/027,215, filed on Feb. 14, 2011, now U.S. Pat.No. 8,318,269, and titled “INDUCTION FOR THERMOCHEMICAL PROCESS, ANDASSOCIATED SYSTEMS AND METHODS;” U.S. patent application Ser. No.13/027,198, filed on Feb. 14, 2011, now U.S. Pat. No. 9,188,086, andtitled “COUPLED THERMOCHEMICAL REACTORS AND ENGINES, AND ASSOCIATEDSYSTEMS AND METHODS;” U.S. Provisional Application No. 61/385,508, filedon Sep. 22, 2010 and titled “REDUCING AND HARVESTING DRAG ENERGY ONMOBILE ENGINES USING THERMAL CHEMICAL REGENERATION;” U.S. patentapplication Ser. No. 13/027,060, filed on Feb. 14, 2011, now U.S. Pat.No. 8,318,100, and titled “REACTOR VESSELS WITH PRESSURE AND HEATTRANSFER FEATURES FOR PRODUCING HYDROGEN-BASED FUELS AND STRUCTURALELEMENTS, AND ASSOCIATED SYSTEMS AND METHODS;” U.S. ProvisionalApplication No. 61/237,419, filed on Aug. 27, 2009 and titled “CARBONSEQUESTRATION;” U.S. patent application Ser. No. 13/027,196, filed onFeb. 14, 2011, now U.S. Pat. No. 8,912,239, and titled “CARBON RECYCLINGAND REINVESTMENT USING THERMOCHEMICAL REGENERATION;” U.S. patentapplication Ser. No. 13/027,195, filed on Feb. 14, 2011, now U.S. Pat.No. 8,784,095, and titled “OXYGENATED FUEL;” U.S. ProvisionalApplication No. 61/237,425, filed on Aug. 27, 2009 and titled“OXYGENATED FUEL PRODUCTION;” U.S. patent application Ser. No.13/027,197, filed on Feb. 14, 2011, now U.S. Pat. No. 8,070,835 andtitled “MULTI-PURPOSE RENEWABLE FUEL FOR ISOLATING CONTAMINANTS ANDSTORING ENERGY;” U.S. Provisional Application No. 61/421,189, filed onDec. 8, 2010 and titled “LIQUID FUELS FROM HYDROGEN, OXIDES OF CARBON,AND/OR NITROGEN; AND PRODUCTION OF CARBON FOR MANUFACTURING DURABLEGOODS”; and U.S. patent application Ser. No. 13/027,185, filed on Feb.14, 2011, now U.S. Pat. No. 8,328,888, and titled “ENGINEERED FUELSTORAGE, RESPECIATION AND TRANSPORT.”

Other Implementations of Methods to Process Carbon-Based Durable Goodsand Renewable Fuels

Techniques, materials, apparatus and systems are described forrepurposing carbon, nitrogen, and hydrogen present in waste streams toproduce durable goods and renewable fuel and store and transport them.For example, carbon-based durable goods, renewable fuels including highdensity hydrogen fuel mixtures, energy including electricity, and othervaluable chemicals, soil nutrients, and materials from organicfeedstocks can be produced using the described processes, systems,materials, and methods.

FIG. 16A shows an exemplary process 1600 that can to producecarbon-based and other durable goods and renewable fuels from organicfeedstocks, which can be stored and transported. Process 1600 caninclude a process 1610 to harvest and subdivide a waste derived from anorganic feedstock, such as a biomass waste from industrial oragricultural processes waste streams. Process 1610 can utilize systemsto recapture and/or recycle low temperature heat (1611) from an externalwaste heat source (e.g., engine exhaust) or a renewable energy source(e.g., solar, wind, hydro, geothermal, etc.). The harvested andsubdivided waste can be preheated (process 1615) and compacted (process1620) before process 1630 that can dry compact the waste, or directlycompacted in process 1630 from process 1610. Process 1630 can remove airand squeeze out moisture (1631), which can include various usefulrenewable sources of carbon and/or hydrogen including hydrocarbons,alcohols, ammonium, and oxides of carbon. Also, the moisture content ofthe overall reaction environment can be controlled based on the desiredrenewable source of carbon and/or hydrogen in process 1640. For example,one method to control the moisture content can include reincorporatingthe compacted biomass waste feedstock that has been completely dried andde-aired into the process 1630 to be used as a desiccant. Other methodscan include use of countercurrent heat exchangers that can utilizerecaptured and/or recycled heat from a waste heat or a renewable energysource. The dried, compacted waste can be dissociated into the wasteconstituents 1651, e.g., at least one of carbon, nitrogen, hydrogen,through process 1650 in an anaerobic dissociation reaction zone. Therenewable sources of hydrogen and carbon can be used to generaterenewable fuel and/or carbon-based durable goods or nitrogen-basedgoods. Process 1600 utilizes a lower temperature heat, and therefore canbe referred to as a “wet stream” process.

Some examples of organic feedstocks include biomass waste. Biomasswastes can derive from various sources, such as rotting wood. Otherexamples include the sourcing of aflatoxin in milk (e.g, M1 and M2aflatoxin in food/feed of lactating animals). The root cause ofaflatoxin can typically be moldy feed—e.g., when moldy feed gets blendedwith a sweetener such as molasses (to make it tasty for the livestock),the toxins produced by the fungal mold source can wind up in milk. Onthe other hand, the moldy feed (biomass waste) can be pretreated withpretreatment process 1625 that can be implemented as an additional stepin the “wet stream” process 1600 as shown in FIG. 16B. Process 1625 caninclude at least one of acid treating, steam treating, or ammoniatreating of the compact preheated waste (from process 1620).Pretreatment process 1625 can further create separable food value andenergy. Additionally, a nitrogen environment can be included in process1625 and used to kill aflatoxin after the mold has produced it by takingwater out of the aflatoxin that dissociates it. To sense aflatoxin ormonitor the amount of nitrogen, for example, one could incorporate andutilize a sensor technique, system, and apparatus, like the sensor andactuator disclosed in U.S. patent application Ser. No. 13/027,188, filedon Feb. 14, 2011, now U.S. Pat. No. 8,312,759, and titled “METHODS,DEVICES, AND SYSTEMS FOR DETECTING PROPERTIES OF TARGET SAMPLES,” inwhich the entirety of its subject matter is incorporated herein byreference. Also a nitrogen environment (e.g., dry nitrogen) can be usedto store things so that there would not be mold or other harmful pests(e.g., insects, rodents, etc.), and thus the use of dissociated nitrogen(obtained in 1631 and 1651) can be employed in this process for storageof food and/or feed.

FIG. 17A shows an exemplary process 1700 that can to producecarbon-based and other durable goods and renewable fuels from organicfeedstocks, which can be stored and transported. Process 1700 caninclude a process 1710 to harvest and subdivide a waste derived from anorganic feedstock, such as a biomass waste from industrial oragricultural processes waste streams. Process 1710 can utilize systemsto recapture and/or recycle high temperature heat (1711) from anexternal waste heat source (e.g., engine exhaust) or a renewable energysource (e.g., concentrated solar, etc.). The harvested and subdividedwaste can be preheated (process 1715) and compacted (process 1720)before process 1730 that can dry compact the waste, or directlycompacted in process 1730 from process 1710. Process 1730 can remove airand squeeze out moisture (1731), which can include various usefulrenewable sources of carbon and/or hydrogen including hydrocarbons,alcohols, ammonium, and oxides of carbon. Also, the moisture content ofthe overall reaction environment can be controlled based on the desiredrenewable source of carbon and/or hydrogen in process 1740. For example,one method to control the moisture content can include reincorporatingthe compacted biomass waste feedstock that has been completely dried andde-aired into the process 1730 to be used as a desiccant. Other methodscan include use of countercurrent heat exchangers that can utilizerecaptured and/or recycled heat from a waste heat or a renewable energysource. The dried, compacted waste can be dissociated into the wasteconstituents 1751, e.g., at least one of carbon, nitrogen, hydrogen,through process 1750 in an anaerobic dissociation reaction zone. Therenewable sources of hydrogen and carbon can be used to generaterenewable fuel and/or carbon-based durable goods or nitrogen-basedgoods. Process 1700 utilizes a high temperature heat, and therefore canbe referred to as a “dry stream” process.

Like process 1600, process 1700 can also include the additional steppretreatment process 1625, including at least one of acid treating,steam treating, or ammonia treating of the compact preheated waste (fromprocess 1720 or 1710 before compacting waste). In addition, the use ofdissociated nitrogen (obtained in 1731 and 1751) can be employed as anitrogen environment in this process for storage of food and/or feed.

In another aspect, renewable energy sources of 1611 and 1711, e.g.,hydroelectric energy, can also be employed to power systems andinfrastructure on a local scale in addition to providing heat to thewaste harvesting processes. This can help to avoid distribution costs,thereby making energy cheaper, and concurrently making a material suchas a carbon-based durable good(s), instead of producing greenhousegases. Factoring economics in a decision process as to whether generateand distribute energy from renewable sources or utilize those renewableenergies to further process durable goods and renewable fuels, or both,on a local scale can consider Energy Park models in the process.

In other aspect of a process to produce carbon-based and other durablegoods and renewable fuels from organic feedstocks, which can be storedand transported, the “dry stream” process can further include a process1770 to separate liquid, gas, solid, after process 1730 to drycompactable waste. Process 1770 can utilize a filter technique, system,and apparatus, such as that disclosed in U.S. patent application Ser.No. 13/027,235, filed on Feb. 14, 2011, now U.S. Pat. No. 8,313,556, andtitled “DELIVERY SYSTEMS WITH IN-LINE SELECTIVE EXTRACTION DEVICES ANDASSOCIATED METHODS OF OPERATION,” in which the entirety of its subjectmatter is incorporated herein by reference. Additionally, process 1770also can utilize a sensor technique, system, and apparatus, such as thatdisclosed in U.S. patent application Ser. No. 13/027,188, filed on Feb.14, 2011, now U.S. Pat. No. 8,312,759, and titled “METHODS, DEVICES, ANDSYSTEMS FOR DETECTING PROPERTIES OF TARGET SAMPLES,” in which theentirety of its subject matter is incorporated herein by reference, inorder to monitor the steps for changing the rate of throughput to matchthe heat input, giving an outcome of selectively (by controlling thetemperature) producing the waste constituents, e.g., methane for thedistribution of carbon and can produce hydrogen. The products ofanaerobic dissociation can include methane. If one chose to distribute aproduct (like a carbon-based durable good (e.g., paraffin substance),then it would be desirable to choose methane; if one chose to distributeenergy, then it would be hydrogen.

Process 1701 can be seen in FIG. 17B. Process 1770 can include anin-line filter, such as the filter referenced above, to carry out theseparation of liquids, gases, and solids into separated wasteconstituents 1771. It is also noted that the sensor and actuatorreferenced above can be utilized at every stage (subprocess) ofprocesses 1600, 1601, 1700, and 1701 in order to monitor the steps forchanging the rate of throughput to match the heat input, giving anoutcome of selectively (by controlling the temperature) producing thewaste constituents, e.g., methane for the distribution of carbon andproduction of hydrogen. The products of anaerobic dissociation caninclude methane. If one chose to distribute a product (like acarbon-based durable good, e.g., paraffin substance), then it would bedesirable to choose methane; if one chose to distribute energy, then itwould be hydrogen.

In another aspect, methane can be put into higher molecular weightsubstances for the purposes of transport and for production, like makingolefin polymers (polyethylene or Poly(4-methyl-1-pentene)). The wayolefins are made to have different properties is by controlling thecrystalline and amorphous percentages (or relative positions incontent), so materials would be very transparent, higher temperaturematerials. To make the strongest fiber in the world, make orientedolefin polyethylene (long, molecular weight oriented); and then to makea higher temperature material, dehydrogenate it (carbon strand). Amethane purification step can be performed in exemplary processes 1600,1601, 1700, and 1701 by taking the methane from 1631 or 1731 if it ispreferred, for example to react CO2 with CH4 to make designer fuels orimpregnating the fuel into architectural constructs. This can make apure methane, not a ‘dirty methane’. For example, a problem with ‘dirtymethane’ is that it inhibits catalytic processes.

In another aspect, an electrolyzer is one of the combination systems tomake much more methane out of the same apparatus, system, or technique(per unit time) and increases throughput by taking away (continuously)acids that are harmful to the microbes; without the acids' inhibition ofthe microbial process, those hydrogen ions (that can be acid producing)can produce both hydrogen and methane. The electrolyzer is a systemwhere, for example, a biomass waste goes to anaerobic dissociationprocess (such as 1650 or 1750). By running the electrolyzer, it can be asource of pressurized hydrogen; the pressurized hydrogen can be used tostir (i.e., change the surface to volume ratio) biodegradeable feedstockfor faster (more efficient) digestion and put hydrogen back into thesystem. Once the ions are divided into atoms and atoms into diatomichydrogen, then it can be bubbled through the liquid environment.

In another aspect, the electrolyzer can also be used in the hightemperature process 1700 and 1701 (in order to use the pressurizedhydrogen and run it back though for stirring). When the excess moistureis squeezed out, the liquid can be run through the electrolyzer tocreate pressurized hydrogen for a stirring device in the anaerobicdissociation process. For example, the liquid that is squeezed out canbe used in electrolyzer for further harvesting, e.g., methane beingliberated (“harvested”), and densified biomass will undergo precisionheating, the byproduct is used a stirring wand.

In another aspect, the electrolyzer can also be used in the lowertemperature process 1600 and 1601. In lower temperature processes usingthe electrolyzer, this can exclude squeeze out or counter-current heatexchange steps. Additionally, the lower temperature process can includethe electrolyzer in anaerobic digestion (“enzymic”), and a third processelectrolysis. Keeping them in the same overall process can be donethrough heat exchange.

Precision heating can be performed with and without vents. For example,with vents: vents can be incorporated in the agar system, placing themat different temperatures, and by relieving the gas trying to escapewith a pathway, it can be collected as methane before it furtherdegrades into hydrogen and carbon. Vents also can give the choice ofharvesting hydrogen or methane during this process.

In another example, without vents: it degrades to hydrogen and carbon.Either with or without the vents, collected gas can come with carbondioxide (because there is oxygen present in the apparatus where theanaerobic process takes place)

In another aspect, harvesting “ash” from 1751 constituents can beperformed so that nutrients for the low temperature process can be used,for example. For example, ash can include trace minerals, such as V, Mg,Ca, Mn, Mo, etc. Microbes can use these minerals to make their enzymes,for example. Therefore, this can feed (as nutrients) back into theanaerobic processes. Ash can be fed back to a third thermochemicalprocess, or the previous thermochemical processes. One can adsorb theseminerals (essentially, the enzymes the microbes use to digest waste) toprevent getting washed away, and can capture them through ‘activatedcarbon.’ The activated carbon can come from the high temperatureproduction of carbon. Microbes can live (as a slime) on the activatedcarbon (e.g., host substrates of activated carbon, otherwiselignocellulose substrates), which can capture and preserve theirenzymes.

A unique opportunity exists to store energy (e.g., hydrogen) insubterranean formation (in most instances, one can pick between warm/hotformation). This process can bring more than one stores. Bringing coldhydrogen to a subterranean surface (that is hot) gives a pressureaddition, a thermal addition, and a chemical addition because it picksup petrochemicals, for example, methane with hydrogen. A furtheradvantage can be that it can enable a spent field (e.g., old oilwells/fields) that has no use economically. Methanol can be delivered tothe surface as “heat”, for example. However, another problem to considerwith geothermal systems can be that water pumped in will mineralize andform carbonates (ex: Mg2+, Ca2+, etc.) and become a poor heat exchanger,no longer a dense heat exchange media. So in such an example, one canreplace the use of water with the use of methanol. Or, in geothermalenergy generation process (instead of water), one can use methanol,ammonia, hydrogen, or CO₂.

Examples of durable goods can include (1) fiber, (2) architecturalconstructs, (3) polymer precursors, (4) plating, (5) intermediates tointermetallics, and (6) diamond.

Further Examples

To reverse global warming carbon is taken from photosynthesizedsubstances including wastes and dangerous clathrates such as methanehydrates and making carbon-enhanced equipment to harness renewableenergy, reduce curb weight for improving fuel economy, and so many otherbetter uses. To further reverse global warming is to utilize theco-produced hydrogen in existing and new engines to replace fossil fuelswith the result of reversing warming by reducing global atmosphericconcentrations of H₂O, CO₂, CH₄, NOx, SOx, H2S etc.

As shown in FIG. 18 global warming gases that would ordinarily bereleased by rotting or burning of carbon in plant tissues can be avoidedby extraction and utilization of such carbon to reinforce, block UVdegradation, and in associated ways provide carbon-enhanced durablegoods. Hydrogen that is coproduced in step 1804 is combined withnitrogen and/or carbon dioxide to produce liquid fuels that denselystore hydrogen such as ammonia or various alcohols as previouslydisclosed. These liquid fuels can be transported by pipelines and storedin tankage previously utilized for fossil fuels such as gasoline ordiesel fuels. This enables engines presently operating throughout theworld to be converted to the hydrogen carrier fuels to provide the netbenefits of improved performance and lower maintenance expenses byoperating on hydrogen. The net impact of such hydrogen combustion isproduction of water vapor in an amount that is less than the amount nowcontributed by fossil fuels that combust fossil-age hydrogen and carbonfrom subterranean storage into the surface inventory of atmosphericgases.

As shown in FIG. 19 global warming that would ordinarily be produced asreleases by permafrost decays and from vast oceanic methane hydratesalong with methane production by municipal and agricultural wastedisposal practices can be profitably avoided. Collected methane can bean economical source of carbon to reinforce and in other ways enhancethe quality and value of durable goods. Hydrogen that is co-producedwith such carbon-enhanced durable goods is combined with nitrogen and/oran oxide of carbon to produce liquid fuels that densely store hydrogensuch as ammonia or various alcohols as previously disclosed. Theseliquid fuels can be transported by pipelines and stored in tankagepreviously utilized for fossil fuels such as gasoline or diesel fuels.This enables efficient deliveries to engines throughout the world forenvironmentally beneficial and improved operations on such hydrogencarrier fuels to provide the net benefit of operating on hydrogen. Thenet impact of such hydrogen combustion is elimination of the carbondioxide and other global warming emissions by utilization of the carbonto produce durable goods and emissions of water vapor in an amount thatis less than the amount now contributed by burning fossil fuels thatremove fossil hydrogen from subterranean storage into the surfaceinventory of gases.

Further, even without counting all the fuel to dig, pump, refine,deliver etc., the hydrogen in a mole of fossil gasoline reacts withoxygen from the air and makes 9 moles of water. FossilC8H18+12.5O2->8CO2+9H2O−plus, the 9 moles of H2O and 8 moles of CO2 areadded to the atmosphere. But methane hydrates or forest slash can bedissociated to produce carbon durable goods and hydrogen instead ofrotting or burning. Using the renewable hydrogen to replace fossil fuelsadds zero water compared to the amount that would have been released bymethane destruction of stratospheric ozone or by plant tissues rottingor burning. And replacing the fossil fuel reduces the atmosphericcontamination by 8 moles of CO2 and 9 moles of H2O. Along withharnessing renewable energy by carbon enhanced equipment this service bya billion engines can provide a much more rapid and profitable relieffor global warming than trying to collect tail pipe CO2 and putting itin the ocean or in deep formations.

EXAMPLES Example 1

Method for reversing global warming comprising

-   -   conversion of carbon dioxide into plant tissue by photosynthesis    -   conversion of plant tissue into carbon enhanced durable goods        and hydrogen collection of at least one of nitrogen or carbon        dioxide from one of the atmosphere or more    -   concentrated sources for reaction with the hydrogen to produce        liquid fuels suitable for replacement of fossil sourced fuels    -   utilization of the liquid fuels in engine selected out of the        world's population of about one billion heat engines to produce        the net result of using hydrogen to power the engines.”

Example 2

The method of Example 1 wherein such liquid fuels are stored in depletedfossil fuel reservoirs.

Example 3

The method of claim Example 2 wherein such liquid fuels are utilized todeliver greater potential energy such as thermal energy, chemicalpotential energy, or pressure potential energy than provided by suchliquid fuel upon entry into such storage.

Example 4

The method of Example 1 wherein such engines use liquid fuels that haveimproved energy density as a result of incorporating architecturalconstruct particles containing hydrogen.

Example 5

Method for reversing global warming comprising conversion of methane,ethane, hydrogen sulfide or carbon dioxide from one of permafrost decay,oceanic clathrates, or waste treatment systems into carbon enhanceddurable goods and hydrogen, wherein

-   -   collection and synthesis of nitrogen or carbon dioxide from the        atmosphere or more concentrated sources with the hydrogen        produces liquid fuels suitable for replacement of fossil sourced        fuels, and    -   utilization of such liquid fuels in selected engines out of the        world's population of about one billion heat engines to produce        the net result of using hydrogen to power the engines.”

Example 6

The method of Example 5 in which such liquid fuels are stored indepleted fossil fuel reservoirs.

Example 7

The method of Example 6 in which such liquid fuels are utilized todeliver greater potential energy from thermal energy, chemical potentialenergy, and or pressure potential energy than provided by such liquidfuel upon entry into such storage.

Example 8

The method of Example 5 in which such engines use liquid fuels that haveimproved energy density as a result of incorporating architecturalconstruct particles containing hydrogen.

CONCLUSION

While this specification contains many specifics, these should not beconstrued as limitations on the scope of any invention or of what may beclaimed, but rather as descriptions of features that may be specific toparticular embodiments of particular inventions. Certain features thatare described in this specification in the context of separateembodiments can also be implemented in combination in a singleembodiment. Conversely, various features that are described in thecontext of a single embodiment can also be implemented in multipleembodiments separately or in any suitable subcombination. Moreover,although features may be described above as acting in certaincombinations and even initially claimed as such, one or more featuresfrom a claimed combination can in some cases be excised from thecombination, and the claimed combination may be directed to asubcombination or variation of a subcombination.

Similarly, while operations are depicted in the drawings in a particularorder, this should not be understood as requiring that such operationsbe performed in the particular order shown or in sequential order, orthat all illustrated operations be performed, to achieve desirableresults. In certain circumstances, multitasking and parallel processingmay be advantageous. Moreover, the separation of various systemcomponents in the embodiments described above should not be understoodas requiring such separation in all embodiments.

Only a few implementations and examples are described and otherimplementations, enhancements and variations can be made based on whatis described and illustrated in this application. For example, thedescribed techniques, systems and apparatus can be implemented toprovide carbon extraction from any hydrogen and carbon containingmaterial. Specific embodiments of the invention have been describedherein for purposes of illustration, but various modifications may bemade without deviating from the spirit and scope of the invention.Accordingly, the invention is not limited except as by the appendedclaims.

To the extent not previously incorporated herein by reference, thepresent application also incorporates by reference in their entirety thesubject matter of each of the following materials: U.S. patentapplication Ser. No. 13/027,235, filed on Feb. 14, 2011, now U.S. Pat.No. 8,313,556, and titled DELIVERY SYSTEMS WITH IN-LINE SELECTIVEEXTRACTION DEVICES AND ASSOCIATED METHODS OF OPERATION; U.S. patentapplication Ser. No. 13/027,188, filed on Feb. 14, 2011, U.S. Pat. No.8,312,759, and titled METHODS, DEVICES, AND SYSTEMS FOR DETECTINGPROPERTIES OF TARGET SAMPLES; U.S. patent application Ser. No.13/027,068, filed on Feb. 14, 2011, now U.S. Pat. No. 8,318,997, andtitled CARBON-BASED DURABLE GOODS AND RENEWABLE FUEL FROM BIOMASS WASTEDISSOCIATION; U.S. patent application Ser. No. 13/027,195, filed on Feb.14, 2011, now U.S. Pat. No. 8,784,095, and titled OXYGENATED FUEL; U.S.patent application Ser. No. 13/027,196, filed on Feb. 14, 2011, now U.S.Pat. No. 8,912,239, and titled CARBON RECYCLING AND REINVESTMENT USINGTHERMOCHEMICAL REGENERATION; U.S. patent application Ser. No.13/027,197, filed on Feb. 14, 2011, now U.S. Pat. No. 8,070,835, andtitled MULTI-PURPOSE RENEWABLE FUEL FOR ISOLATING CONTAMINANTS ANDSTORING ENERGY; and U.S. patent application Ser. No. 13/027,185, filedon Feb. 14, 2011, now U.S. Pat. No. 8,328,888, and titled ENGINEEREDFUEL STORAGE, RESPECIATION AND TRANSPORT.

I claim:
 1. A method to produce a renewable fuel or a carbon byproduct,or both, from a waste source, the method comprising: obtaining anorganic feedstock derived from a waste produced by at least one of anindustrial or agricultural process; heating the organic feedstock wastewith a low temperature heat recovered from a waste heat source;compacting the low temperature-heated organic feedstock waste; removingmoisture from the compacted and low temperature-heated organic feedstockwaste to produce substantially dried organic feedstock; dissociating thesubstantially dried organic feedstock by an anaerobic reaction toproduce waste constituents including hydrogen and at least one of carbondonors or nitrogen donors, wherein the dissociating includes usingmicrobes in the anaerobic reaction to dissociate the substantially driedorganic feedstock and using an electrolyzer system to providepressurized hydrogen to the anaerobic reaction and remove acidicconstituent by-products; and reacting the hydrogen with at least one ofthe carbon donors or nitrogen donors to generate the renewable fuel orthe carbon byproduct, or both.
 2. The method of claim 1, wherein the lowtemperature heat is recovered by at least one of: capturing heatrejected from an engine, or generating heat from a renewable energygenerator including at least one of a wind energy generator, a solarenergy generator, a hydro energy generator, or a geothermal energygenerator.
 3. The method of claim 1, further comprising: subdividing theorganic feedstock into a plurality of groups of the organic feedstock.4. The method of claim 1, wherein the removing the moisture includespartially removing some moisture from the compacted and lowtemperature-heated organic feedstock waste, thereby preserving aparticular amount of the moisture in the compacted and lowtemperature-heated organic feedstock waste.
 5. The method of claim 1,wherein the waste includes biomass waste, and the organic feedstockincludes at least one of rotted wood or livestock feed.
 6. The method ofclaim 1, further comprising: storing the waste constituents in a storagelocated in a first location; and transporting at least some of the wasteconstituents to a second location to implement the reacting to generatethe renewable fuel or the carbon byproduct, or both.
 7. A method toproduce a renewable fuel or a carbon byproduct, or both, from a wastesource, the method comprising: obtaining an organic feedstock derivedfrom a waste produced by at least one of an industrial or agriculturalprocess; heating the organic feedstock waste with a high temperatureheat recovered from a waste heat source to remove moisture from theorganic feedstock waste to produce substantially dried organicfeedstock; compacting the substantially dried organic feedstock;dissociating the substantially dried organic feedstock by an anaerobicreaction to produce waste constituents including hydrogen and at leastone of carbon donors or nitrogen donors, wherein the dissociatingincludes using microbes in the anaerobic reaction to dissociate thesubstantially dried organic feedstock and using an electrolyzer systemto provide pressurized hydrogen to the anaerobic reaction and removeacidic constituent by-products; and reacting the hydrogen with at leastone of the carbon donors or nitrogen donors to generate the renewablefuel or the carbon byproduct, or both, wherein the high temperature heatis recovered by at least one of capturing heat rejected from an engine,or generating heat from a renewable energy generator including at leastone of a wind energy generator, a solar energy generator, a hydro energygenerator, or a geothermal energy generator.
 8. The method of claim 7,wherein the waste includes biomass waste, and the organic feedstockincludes at least one of rotted wood or livestock feed.
 9. The method ofclaim 7, further comprising: storing the waste constituents in a storagelocated in a first location; and transporting at least some of the wasteconstituents to a second location to implement the reacting to generatethe renewable fuel or the carbon byproduct, or both.